CN210505915U - High enriched waste water zero release processing apparatus - Google Patents

High enriched waste water zero release processing apparatus Download PDF

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CN210505915U
CN210505915U CN201920840410.5U CN201920840410U CN210505915U CN 210505915 U CN210505915 U CN 210505915U CN 201920840410 U CN201920840410 U CN 201920840410U CN 210505915 U CN210505915 U CN 210505915U
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黄小雷
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Dongguan Xinyi Glasses Manufacture Co ltd
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Abstract

The utility model relates to a high enriched waste water zero release processing apparatus, including pretreatment mechanism, second filter mechanism, second MCR system, STUF membrane system, first filter mechanism, first MCR system, resin exchange system, charcoal that communicate in proper order strain system, UF membrane system and tertiary reverse osmosis Ro membrane processing system. The utility model provides a high enriched waste water 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

High enriched waste water zero release processing apparatus
Technical Field
The utility model belongs to the technical field of sewage treatment plant, concretely relates to high enriched waste water 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 high-concentration wastewater zero-discharge treatment device. The utility model provides a processing apparatus carries out the pertinence to high enriched waste water and handles, 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 is 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 high-concentration wastewater zero-emission treatment device comprises a pretreatment mechanism, a second filtering mechanism, a second MCR system, an STUF membrane system, a first filtering mechanism, a first MCR system, a resin exchange system, a carbon filtering system, an UF membrane system and a three-stage reverse osmosis Ro membrane treatment system which are sequentially communicated; 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.
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 inorganic salt and heavy metal pollutants are concentrated, separated and dissolved, organic matters and conductivity in the evaporated effluent are greatly reduced, and then coarse filtration is carried out by utilizing a first filtering part to remove large particles and silt in the wastewater, and secondary filtration is carried out by utilizing a first MCR system. 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.
Specifically, utilize the utility model provides a process that processing apparatus carries out processing to electroplating effluent is as follows:
adjusting the pH value of the high-concentration wastewater to 3-4, adding a reducing agent, adjusting the pH value 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 Filter Membrane) system technology, performing rough filtration on evaporated and separated effluent, performing secondary filtration by using the MCR technology, performing ion exchange by using anion resin and cation resin, performing carbon filtration, and sequentially performing UF membrane treatment and three-stage reverse osmosis Ro membrane treatment, wherein the Ro produced water is the recyclable water quality, and the Ro concentrated water is used as the high-concentration wastewater for subsequent treatment. 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 high enriched waste water 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.
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 effluent from the STUF membrane system can be collected by a water collecting tank and subjected to subsequent treatment.
More preferably, a water pump is communicated between the water collecting tank and the first filtering mechanism.
The water pump can realize that the water outlet of the STUF membrane system in the water collecting tank is pumped into the first filtering mechanism.
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 system (e.g., LGJ1E3-1500 x 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 (e.g., 1000X1850X4X 4).
Preferably, the UF membrane system is a vertical liter ultrafiltration membrane module (e.g., 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 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 carries out the pertinence to high enriched waste water and handles, 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 is 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, 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; b is high-concentration 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 the electroplating sewage, and collecting the wastewater generated in the cleaning step as cleaning wastewater; 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 measurement of the high concentration wastewater are shown in Table 1.
TABLE 1 quality of wastewater in examples
Figure BDA0002082832230000051
Example 1
The present embodiment provides a high-concentration wastewater zero-emission treatment device, as shown in fig. 1, which includes a pretreatment mechanism 9, a second filtration mechanism 10, a second MCR system 11 (in the present embodiment, LGJ1E-1500 × 6), an STUF membrane system 12 (in the present embodiment, LGJ 1-1E-1500 × 14), a sump, a water pump, a first filtration mechanism 1, a first MCR system 2 (in the present embodiment, LGJ 1-E-1500 × 14), a resin exchange system (3), a carbon filtration system 4 (in the present embodiment, 1000X1850-4-4), a UF membrane system 5 (in the present embodiment, LH3-1060-V), and a three-stage reverse osmosis ropa membrane treatment system 6 (in the present embodiment, No. LH 3-LD8040) that 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 a 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 a pretreatment water tank of a triple-effect evaporator; the water outlet of the DTRO secondary concentration mechanism is communicated with the first filtering mechanism 1. The concentrated water of the triple-effect evaporator can be transported and treated. The first filtering mechanism 1 is a rough filtering mechanism, and specifically is an activated 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.
The process of treating high concentration wastewater by using the treatment apparatus provided in this example is as follows.
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 method comprises the following steps that water produced by an STUF membrane system enters a buffer water tank of the STRO system, the water enters the STRO system after being pumped through a security filter at high pressure by the buffer water tank and is pre-concentrated to separate and dissolve inorganic salt and heavy metal pollutants, the produced water enters a primary water tank of a three-level Ro, concentrated water enters a buffer water tank of the DTRO system, the concentrated water enters the DTRO system after being pumped through the security filter at high pressure by the buffer water tank and is secondarily concentrated, the produced water of the DTRO system enters the primary water tank of the three-level Ro, the concentrated water enters an evaporation treatment pre-treatment water tank, concentrated solution enters a three-effect evaporator preheater through an evaporation system in a vacuum self-suction manner, the concentrated solution enters a three-effect evaporator separator after being evaporated by the three-effect evaporator, condensed water is pumped to a water collecting tank through a condensed water pump and is lifted to an active carbon filter by the; the wastewater after the pretreatment enters a resin exchange system through a bag filter, and cation resin (TP-207) is utilized to carry 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.
The total water quality of the treated high-concentration wastewater was measured, and the results are shown in Table 2.
TABLE 2 Total Water quality after treatment
Figure BDA0002082832230000071
From the above, the utility model provides a processing apparatus carries out the pertinence to high concentration waste water and handles, selects for use the full physical separation process systems who only introduces a small amount of external medicaments, can reach the 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 high-concentration wastewater zero-emission treatment device is characterized by comprising a pretreatment mechanism (8), a second filtering mechanism (9), a second MCR system (10), an STUF membrane system (11), a first filtering mechanism (1), a first MCR system (2), a resin exchange system (3), a carbon filtering system (4), an UF membrane system (5) and a three-level reverse osmosis Ro membrane treatment system (6) which are sequentially communicated; 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 high-concentration wastewater zero-discharge treatment device according to claim 1, characterized in that the first filtering mechanism (1) and the second filtering mechanism (9) are both coarse filtering mechanisms.
3. The high concentration wastewater zero discharge 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 high-concentration wastewater zero-discharge treatment device according to claim 1, characterized in that the resin exchange system (3) comprises a negative resin and a positive resin.
5. The high-concentration wastewater zero-discharge treatment device according to claim 1, wherein the number of the negative resins is multiple groups, and the number of the positive resins is multiple groups.
6. The high-concentration wastewater 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 is (5) a vertical-liter ultrafiltration membrane group.
7. The high-concentration 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 three-effect evaporator preheater and a three-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.
8. The high concentration wastewater zero discharge treatment device according to claim 1, wherein the pretreatment tank mechanism (8) comprises a reduction tank, a pH adjustment tank and a sedimentation tank.
9. The high concentration wastewater zero discharge treatment device according to claim 1, wherein the second MCR system (11) comprises a produced water collection tank and a bag filter, wherein 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 high-concentration wastewater zero-emission treatment device 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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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112047553A (en) * 2020-09-18 2020-12-08 新疆中泰创新技术研究院有限责任公司 PTA high-salinity wastewater treatment, reuse and zero-discharge system and method

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112047553A (en) * 2020-09-18 2020-12-08 新疆中泰创新技术研究院有限责任公司 PTA high-salinity wastewater treatment, reuse and zero-discharge system and method

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