CN214141919U - Concentrated liquid processing system of leachate - Google Patents
Concentrated liquid processing system of leachate Download PDFInfo
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- CN214141919U CN214141919U CN202022380698.8U CN202022380698U CN214141919U CN 214141919 U CN214141919 U CN 214141919U CN 202022380698 U CN202022380698 U CN 202022380698U CN 214141919 U CN214141919 U CN 214141919U
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Abstract
The utility model belongs to solution treatment facility field, concretely relates to leachate concentrate processing system, include: the system comprises a raw water pool for storing percolate concentrated solution, a high-pressure nanofiltration salt separation unit, an electrodialysis unit and a reverse osmosis water treatment unit which are sequentially connected with the raw water pool; the high-pressure nanofiltration salt separation unit is suitable for intercepting macromolecular organic matters and ions with more than two valences in the percolate concentrated solution to form primary concentrated solution and primary produced water; the electrodialysis unit is adapted to migrate a majority of remaining ions in the primary product water to form secondary product water; the reverse osmosis water treatment unit is suitable for further removing ions in the secondary produced water to form a final concentrated solution and final produced water. Macromolecular organic matters and ions in the percolate concentrated solution are gradually removed by sequentially processing the percolate concentrated solution with specific components, so that the discharge standard is reached.
Description
Technical Field
The utility model relates to a solution treatment facility field, concretely relates to leachate concentrate processing system.
Background
At the present stage, the landfill leachate treatment process generally adopts pretreatment, anaerobism, MBR and a double-membrane method, although the process can stably discharge up to the standard, a large amount of concentrated solution can be generated at the same time, and the concentrated solution contains extremely high salinity, so that the salinity can return to the system if recharging is carried out, a large amount of accumulation of the salinity is caused, the leachate treatment system is influenced, and the leachate concentrated solution cannot go anywhere. The currently adopted main stream concentrated solution treatment process is high pressure reverse osmosis (DTRO) for concentrated water reduction, and the rest 20-25% of concentrated water is subjected to pretreatment and evaporation. The process carries out evaporation after simple pretreatment, and has the following problems: 1) because the concentrated solution contains a large amount of organic matters and hardness, the evaporator is often subjected to scaling, blockage and severe environment, and salt cannot be evaporated; 2) the tail gas has large odor and great treatment difficulty, and influences the surrounding environment; 3) the investment and the operation cost are huge, the investment per ton of water of the system is usually up to 10 ten thousand yuan, and the direct operation cost per ton of water can be up to more than 100 yuan.
For example, patent 201710651539.7 discloses a method for realizing near-zero emission of reverse osmosis concentrated water, which comprises sequentially subjecting raw water to reverse osmosis concentration and separation, nanofiltration separation, chemical softening, bipolar membrane electrodialysis, etc. Wherein, reverse osmosis concentration separation: the pretreated raw water enters a reverse osmosis concentration separation system for concentration separation to obtain fresh water and reverse osmosis concentrated water; nanofiltration separation: the reverse osmosis concentrated water enters a nanofiltration membrane treatment system, and the nanofiltration membrane treatment system intercepts high-valence ions to obtain nanofiltration effluent and nanofiltration concentrated water; chemical softening: the nanofiltration concentrated water enters a chemical softening system to be neutralized by acid and alkali to obtain neutralized effluent; softening of sodium resin: the neutralized effluent enters a sodium resin softening device for sodium ion exchange, and high-valence metal cations are removed to obtain sodium resin softened effluent; bipolar membrane electrodialysis: and the softened effluent of the sodium resin enters a bipolar membrane electrodialysis device for electrodialysis to produce acid, alkali and bipolar membrane effluent. The method for realizing near-zero emission of the osmosis concentrated water still has the defects of high investment, inconvenience in use and the like because no chemical components of the percolate concentrated solution have no pertinence, the problem is relieved to a limited extent only by improving the recovery and utilization of the reverse osmosis concentrated water, and the problems of overhigh operation cost and investment cost are not solved comprehensively.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a concentrated liquid processing system of infiltration liquid handles in proper order to the concentrated liquid of infiltration liquid of specific composition, progressively gets rid of macromolecular organic matter and ion in the concentrated liquid of infiltration liquid to reduce follow-up evaporation unit's handling capacity.
In order to solve the above technical problem, the utility model provides a percolate concentrate processing system, include: the system comprises a raw water pool for storing percolate concentrated solution, a high-pressure nanofiltration salt separation unit, an electrodialysis unit and a reverse osmosis water treatment unit which are sequentially connected with the raw water pool; the high-pressure nanofiltration salt separation unit is suitable for intercepting macromolecular organic matters and ions with more than two valences in the percolate concentrated solution to form primary concentrated solution and primary produced water; the electrodialysis unit is adapted to migrate a majority of remaining ions in the primary product water to form secondary concentrate water, secondary product water; the reverse osmosis water treatment unit is suitable for further removing ions in the secondary produced water to form a final concentrated solution and final produced water.
Further, the high pressure nanofiltration salt separation unit comprises: a primary water outlet and a primary concentrated solution outlet; wherein the primary produced water flows from the primary produced water outlet into the electrodialysis unit; the primary concentrate enters the improved conditioning unit from the primary concentrate outlet.
Further, the improvement adjusting unit includes: the advanced oxidation tank, the coagulating sedimentation tank and the percolate adjusting tank are connected in sequence; wherein the advanced oxidation pond is suitable for improving the COD which is difficult to degrade in the primary concentrated solution; the coagulating sedimentation tank is suitable for removing the hardness of the primary concentrated solution; the percolate adjusting tank is suitable for adjusting the primary concentrated solution.
Further, the percolate concentrate treatment system also comprises a biochemical unit connected with the percolate regulating tank.
Further, the electrodialysis unit comprises: a fresh water chamber and a concentrated water chamber; most of the ions in the primary product water migrate into the concentrate chamber to form the secondary concentrate water and the secondary product water in the dilute chamber.
Further, the reverse osmosis water treatment unit comprises: a discharge port, a circulation pipe; wherein the final stage produced water is discharged from the discharge port; and the final-stage concentrated solution enters a raw water pool through a circulating pipeline.
The beneficial effects of the utility model are that, the utility model discloses a percolate concentrate processing system handles in proper order the percolate concentrate of specific composition, progressively gets rid of macromolecule organic matter and ion in the percolate concentrate to the unable problem of handling or the processing cost height of percolate concentrate has been solved.
Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and drawings.
In order to make the aforementioned and other objects, features and advantages of the present invention comprehensible, preferred embodiments accompanied with figures are described in detail below.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic block diagram of a permeate concentrate processing system of the present invention.
Detailed Description
To make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and obviously, the described embodiments are some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
As shown in fig. 1, the present embodiment provides a diafiltration concentrate processing system comprising: a raw water tank for storing percolate concentrated solution, a high-pressure nanofiltration salt separation unit (DTNF), an electrodialysis unit (ED) and a reverse osmosis water treatment unit (RO) which are sequentially connected with the raw water tank; the high-pressure nanofiltration salt separation unit is suitable for intercepting macromolecular organic matters and ions with more than two valences in the percolate concentrated solution to form primary concentrated solution and primary produced water; the electrodialysis unit is adapted to migrate a majority of remaining ions in the primary product water to form secondary concentrate water, secondary product water; the reverse osmosis water treatment unit is suitable for further removing ions in the secondary produced water to form a final concentrated solution and final produced water.
Optionally, the percolate concentrate includes, but is not limited to, landfill leachate subjected to front-end pretreatment and biochemical treatment, which removes most of COD and ammonia nitrogen, and also contains a large amount of macromolecular COD (chemical oxygen demand), TDS (total dissolved solids), chloride ions, and a small amount of nitrate nitrogen, nitrite nitrogen, and hardness.
As an alternative embodiment of the high pressure nanofiltration salt separation unit.
The high-pressure nanofiltration salt separation unit comprises: a primary water outlet and a primary concentrated solution outlet; wherein the primary produced water flows from the primary produced water outlet into the electrodialysis unit; the primary concentrate enters the improved conditioning unit from the primary concentrate outlet.
Optionally, the high-pressure nanofiltration salt separation unit can select a ceramic membrane or a butterfly-tube nanofiltration membrane, has low requirement on the quality of inlet water, and can be suitable for treating wastewater with high hardness, high organic matters and high salinity; the method is similar to NF (NF is a novel molecular-level membrane separation technology between ultrafiltration and reverse osmosis, and is a membrane process suitable for separating dissolved components with molecular weights of more than 200 and molecular sizes of about 1 nm), the rejection rate of monovalent ions is low, macromolecular organic matters and ions with more than two valences are mainly intercepted, so that most of COD, hardness, a small amount of chloride ions and ammonia nitrogen in concentrated solution of percolate can be intercepted, the water yield of DTNF can reach 80%, most of primary produced water is monovalent salt, mainly comprises chloride ions, nitrate radicals and nitrite and cannot reach the standard, so that primary produced water is introduced into an electrodialysis unit for further treatment, primary concentrated solution mainly comprises macromolecular COD and hardness, and an adjusting unit can be improved for treatment.
Further, referring to fig. 1, the improvement adjusting unit includes: the advanced oxidation tank, the coagulating sedimentation tank and the percolate adjusting tank are connected in sequence; wherein the advanced oxidation pond is suitable for improving the COD which is difficult to degrade in the primary concentrated solution; the coagulating sedimentation tank is suitable for removing the hardness of the primary concentrated solution; the leachate adjusting tank is internally provided with a stirrer which has the function of average value and can adjust and treat primary concentrated solution. Specifically, the primary concentrated solution adopts advanced oxidation treatment (such as Fenton, electrocatalytic oxidation, ozone and other treatment modes), COD which is difficult to degrade in the primary concentrated solution can be improved, after the hardness of the primary concentrated solution is removed through coagulating sedimentation (by adding polyacrylamide PAM and polyaluminium chloride PAC), produced water is pumped back to a percolate adjusting tank and then is connected to a biochemical unit for treatment, wherein the biochemical tank mainly plays a role in denitrification, and the common mode is an A/O system.
As an alternative embodiment of the electrodialysis unit.
The electrodialysis unit comprises: a fresh water chamber and a concentrated water chamber; most of the ions in the primary product water migrate into the concentrate chamber to form the secondary concentrate water and the secondary product water in the dilute chamber.
Optionally, the electrodialysis unit (ED) may be an ASTOM membrane, which is a membrane separation process using an electric field as a driving force, and desalination and concentration of ions are achieved by using selective permeability of an ion exchange membrane. By controlling the conductance of the fresh water chamber, most ions (chloride ions, nitrate radicals, nitrite radicals and the like) are transferred to the concentrated water chamber, and the water yield of ED can reach 80%; but because ED has no interception to COD and part of ions still exist in the fresh water chamber, the secondary produced water still does not reach the discharge standard and needs to enter a reverse osmosis water treatment unit for further treatment. The secondary concentrated water in the concentrated water chamber is mainly monovalent salt, and COD and hardness are very little, so the secondary concentrated water can be directly connected into an evaporator for treatment without the risk of scaling and incapability of crystallizing.
As an alternative embodiment of the evaporation unit.
The evaporation unit comprises an evaporator connected with the concentrated water chamber.
As an alternative embodiment of the reverse osmosis water treatment unit.
The reverse osmosis water treatment unit comprises: a discharge port, a circulation pipe; wherein the final stage produced water is discharged from the discharge port; and the final-stage concentrated solution enters a raw water pool through a circulating pipeline.
Optionally, the reverse osmosis water treatment unit (RO) may select a dow membrane to remove COD, ammonia nitrogen, and other small amounts of heavy metals that may be present in the secondary product water, so that the final product water reaches the discharge standard, and at the same time, the final concentrate only contains a part of COD, heavy metals, and a small amount of salts, so that it can be returned to the raw water tank through a circulation pipeline to be mixed with the percolate concentrate for further treatment.
In the scheme, the high-pressure nanofiltration salt separation unit, the electrodialysis unit and the reverse osmosis water treatment unit are all in the prior art, and the structure of the high-pressure nanofiltration salt separation unit, the electrodialysis unit and the reverse osmosis water treatment unit is not substantially improved, so that the high-pressure nanofiltration salt separation unit, the electrodialysis unit and the reverse osmosis water treatment unit do not belong to the protection range of the scheme. In the scheme, according to the chemical components or the processing requirements of the percolate concentrate, a proper filtering membrane can be selected, and the percolate concentrate is sequentially processed through all the components, so that the percolate concentrate is processed step by step. And the percolate concentrated solution and all levels of produced water and concentrated solution generated by the percolate concentrated solution can be conveyed through corresponding pipelines, and corresponding switch valves can be arranged among all components according to requirements.
To sum up, the utility model discloses a concentrated liquid processing system of infiltration liquid adopts DTNF, ED, RO to the concentrated liquid of infiltration liquid in proper order, adopts advanced oxidation, coagulating sedimentation, the treatment process that the filtration liquid equalizing basin combines to the elementary concentrate that DTNF produced simultaneously in proper order, and the rate of recovery of this system can reach 80%, and only 20% concentrated liquid of infiltration liquid (secondary concentrated water promptly) carry out evaporation treatment, has both reduced evaporation unit's handling capacity, makes the stable up to standard of water outlet, has greatly reduced investment and working costs again. The percolate concentrate treatment system also has the following advantages:
1) because the investment and operation cost of the evaporation ton is too high, the percolate concentrate treatment system greatly reduces the amount of concentrate entering an evaporation unit, thereby greatly reducing the investment and operation cost;
2) in the process of treating the percolate concentrated solution, COD, hardness and the like which influence the stable operation of the evaporation unit are removed in the high-pressure nanofiltration salt separation unit, so that the stable operation of the evaporation unit is ensured, and no odor is generated.
In the description of the embodiments of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the several embodiments provided in the present application, it should be understood that the disclosed system, apparatus and method may be implemented in other ways. The above-described embodiments of the apparatus are merely illustrative, and for example, the division of the units is only one logical division, and there may be other divisions when actually implemented, and for example, a plurality of units or components may be combined or integrated into another system, or some features may be omitted, or not executed.
In light of the foregoing, it will be apparent to those skilled in the art from this disclosure that various changes and modifications can be made without departing from the spirit and scope of the invention. The technical scope of the present invention is not limited to the content of the specification, and must be determined according to the scope of the claims.
Claims (7)
1. A diafiltration concentrate processing system, comprising:
the system comprises a raw water pool for storing percolate concentrated solution, a high-pressure nanofiltration salt separation unit, an electrodialysis unit and a reverse osmosis water treatment unit which are sequentially connected with the raw water pool; wherein
The high-pressure nanofiltration salt separation unit is suitable for intercepting macromolecular organic matters and ions with more than two valences in the percolate concentrated solution to form primary concentrated solution and primary produced water;
the electrodialysis unit is adapted to migrate a majority of remaining ions in the primary product water to form secondary concentrate water, secondary product water;
the reverse osmosis water treatment unit is suitable for further removing ions in the secondary produced water to form a final concentrated solution and final produced water;
the high-pressure nanofiltration salt separation unit is a Dow membrane.
2. The diafiltration concentrate processing system of claim 1,
the high-pressure nanofiltration salt separation unit comprises: a primary water outlet and a primary concentrated solution outlet; wherein
The primary produced water flows into the electrodialysis unit from the primary produced water outlet;
the primary concentrate enters the improved conditioning unit from the primary concentrate outlet.
3. The diafiltration concentrate processing system according to claim 2,
the improvement adjustment unit includes: the advanced oxidation tank, the coagulating sedimentation tank and the percolate adjusting tank are connected in sequence; wherein
The advanced oxidation pond is suitable for improving the COD which is difficult to degrade in the primary concentrated solution;
the coagulating sedimentation tank is suitable for removing the hardness of the primary concentrated solution;
the percolate adjusting tank is suitable for adjusting the primary concentrated solution.
4. The diafiltration concentrate processing system of claim 3,
the percolate concentrate treatment system further comprises a biochemical unit connected with the percolate regulating tank.
5. The diafiltration concentrate processing system according to claim 2,
the electrodialysis unit comprises: a fresh water chamber and a concentrated water chamber;
most of the ions in the primary product water migrate into the concentrate chamber to form the secondary concentrate water and the secondary product water in the dilute chamber.
6. The diafiltration concentrate processing system of claim 5,
the diafiltration concentrate treatment system also includes an evaporation unit connected to the concentrate chamber.
7. The diafiltration concentrate processing system according to claim 5, wherein the reverse osmosis water treatment unit comprises: a discharge port, a circulation pipe; wherein
Discharging final-stage produced water from a discharge port;
and the final-stage concentrated solution enters a raw water pool through a circulating pipeline.
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| CN202022380698.8U CN214141919U (en) | 2020-10-22 | 2020-10-22 | Concentrated liquid processing system of leachate |
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| CN202022380698.8U CN214141919U (en) | 2020-10-22 | 2020-10-22 | Concentrated liquid processing system of leachate |
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