CN216038723U - MVR evaporation system for concentrated solution treatment - Google Patents
MVR evaporation system for concentrated solution treatment Download PDFInfo
- Publication number
- CN216038723U CN216038723U CN202121213312.2U CN202121213312U CN216038723U CN 216038723 U CN216038723 U CN 216038723U CN 202121213312 U CN202121213312 U CN 202121213312U CN 216038723 U CN216038723 U CN 216038723U
- Authority
- CN
- China
- Prior art keywords
- concentrated solution
- evaporation
- stage
- forced evaporator
- stage forced
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model belongs to the technical field of garbage treatment, and particularly relates to an MVR evaporation system for treating concentrated solution, which comprises: a pretreatment mechanism for pretreating the concentrated solution; the low-temperature MVR evaporation mechanism is used for carrying out low-temperature MVR evaporation on the pretreated concentrated solution to generate crystalline salt, mother liquor and condensed water; the filtering mechanism is used for filtering the condensed water after the low-temperature MVR is evaporated so as to form clear liquid to be discharged; the concentrated solution is pretreated by the pretreatment mechanism, high-boiling-point organic matter components (mainly humus which is difficult to degrade) in the inlet water of the concentrated solution can be removed, so that the high-efficiency separation of the organic matter and the salt is realized, the evaporation maintenance cost is reduced, the low-temperature MVR evaporation mechanism is adopted, the operation temperature is in the range of 55-70 ℃, the stable operation of evaporation can be ensured, the safety coefficient is properly reserved, the stable operation, energy conservation and environmental protection are realized, and the qualified discharge is ensured by filtering the condensed water by the filtering mechanism.
Description
Technical Field
The utility model belongs to the technical field of garbage treatment, and particularly relates to an MVR evaporation system for treating concentrated solution.
Background
The landfill leachate refers to a high-concentration organic or inorganic liquid generated by biochemical degradation of garbage due to compaction, fermentation and the like in the stacking and landfill processes and under the seepage action of precipitation and underground water, and almost all the landfill leachate is from landfill sites and incineration plants at present.
The landfill leachate contains various toxic and harmful inorganic matters and organic matters due to complex components, and also contains non-chlorinated aromatic compounds such as naphthalene and phenanthrene, chlorinated aromatic compounds, phosphoric acid vinegar, phenolic compounds, aniline compounds and the like which are difficult to biodegrade. The highest concentration of CODcr and BOD5 in the landfill leachate can reach thousands to tens of thousands, and compared with municipal sewage, the concentration is much higher, so the leachate can not be directly discharged into a municipal sewage treatment pipeline without strict treatment and disposal. In general, CODcr, BOD5, BOD5/CODcr decrease with "age" of the landfill and alkalinity levels increase. Therefore, the landfill leachate can be discharged after being treated.
At present, landfill sites and incineration plant leachate are treated in a plurality of comprehensive ways, and the landfill sites and the incineration plant leachate are generally pretreated in the early stage, then treated in the anaerobic stage and then treated in the aerobic stage, and then subjected to ultrafiltration, nanofiltration and reverse osmosis. The ultrafiltration can filter out macromolecules and suspended matters, the main components of the ultrafiltration membrane are humic acid, various micromolecules, Ca2+, Mg2+, Na +, Cl-, CO2-, SO 42-and the like, and the ultrafiltration needs to be further treated; almost all humic acid and bivalent and above ions are separated out by the nanofiltration membrane, and the separated concentrated solution accounts for about 20 percent of that entering the nanofiltration. The nanofiltration concentrate is not easy to store or bury due to high salinity and organic matter concentration, and needs further treatment. The solution penetrating the nanofiltration membrane still needs further treatment because the solution contains higher monovalent ions such as Na < + >, Cl < - >, and the like, which do not reach the emission standard, and therefore, a reverse osmosis process is also needed. The clear liquid after reverse osmosis treatment can be discharged or used for irrigation of public utilities and the like after reaching the discharge standard, the reverse osmosis concentrated solution accounts for about 25 percent of the total amount entering a reverse osmosis system, and the main components are solutions of monovalent ions such as Na +, Cl & lt- & gt and the like.
For the reverse osmosis concentrated solution, because the pollution is low, a natural air drying and then landfill mode can be adopted, but the efficiency is low by the natural air drying, and the occupied area is large; the industrial salt can also be processed by the process, but the cost is higher; evaporation can be promoted in a heat treatment concentration mode, but the heat exchange contact surface is easy to crystallize due to improper heat treatment process, so that uneven heat conduction of the heating surface and reduced heat exchange effect are caused.
For the treatment of nanofiltration concentrated solution, some processes adopt reflux to enter a leachate treatment system again, although the total amount of humic acid can be reduced by adopting the mode, the concentration of Ca2+, Mg2+, CO2-, SO 42-and other ions is increased along with the increase of the circulation times, and the influence is caused on the leachate treatment system before nanofiltration, SO that the reflux cannot finally solve the nanofiltration concentrated solution; spraying the waste incineration furnace hearth can cause corrosion and scaling damage to the heating surface; the leachate is finally re-introduced into the landfill.
Nanofiltration concentrate and reverse osmosis concentrate are collectively referred to as membrane concentrate. At present, typical methods for treating membrane concentrated solution at home and abroad include a recharging method and an evaporation method. But some problems have been found in practical applications. The recharging method can improve the recovery rate and increase the washing flow rate of the membrane surface; however, the drawback of recharging gradually appears along with the lapse of time, and the domestic refuse landfill sites have the problems of accumulation of pollutants in different degrees, increase of the conductivity of percolate, reduction of the water yield of the membrane, and even failure of membrane filtration caused by the increase of the conductivity.
The evaporation method is a process of separating out relatively volatile components in a mixed solution under certain temperature and pressure. The evaporation treatment process can concentrate the volume of the solution to be treated to be less than 2-10% of the volume of the original solution. The evaporation comprises normal-pressure high-temperature evaporation, novel heat pump evaporation and the like, and the normal-pressure high-temperature evaporation process has the same problem of equipment corrosion in the actual operation process. This has become the most important limiting factor for the atmospheric high-temperature evaporation treatment of landfill leachate or membrane concentrate. The novel heat pump evaporation belongs to vacuum evaporation, a vacuum evaporation method needs to be provided with vacuum pumping equipment, and an evaporation concentration system needs to have good pressure bearing performance and sealing performance, so that the system is high in design, manufacture, installation and operation requirements, and high in initial investment and operation cost, and further does not have mature large-scale application.
Therefore, there is a need to develop a new MVR evaporation system for concentrate treatment to solve the above problems.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide an MVR evaporation system for treating concentrated solution so as to solve the problem of how to separate crystal salt, mother solution and condensed water from the concentrated solution.
In order to solve the above technical problem, the present invention provides an MVR evaporation system for concentrated solution treatment, comprising: a pretreatment mechanism for pretreating the concentrated solution; the low-temperature MVR evaporation mechanism is used for carrying out low-temperature MVR evaporation on the pretreated concentrated solution to generate crystalline salt, mother liquor and condensed water; and the filtering mechanism is used for filtering the condensed water after the low-temperature MVR is evaporated so as to form clear liquid to be discharged.
Further, the pre-processing mechanism comprises: a feed tank and a material film at an inlet of the feed tank; the material membrane is suitable for filtering the concentrated solution entering the feeding tank to remove high-boiling-point organic matter components in the concentrated solution.
Further, the low temperature MVR evaporation mechanism includes: a feed pump, a two-stage plate preheater and an evaporation chamber; the feed pump is suitable for pumping the concentrated solution in the feed tank into the two-stage plate type preheater for preheating, namely the concentrated solution enters the evaporation chamber for two-stage concentration and evaporation after being preheated to be close to a bubble point so as to generate crystalline salt, concentrated mother liquor and condensed water.
Further, a first-stage forced evaporator and a second-stage forced evaporator are arranged in the evaporation chamber; the preheated concentrated solution enters a first-stage forced evaporator, the temperature of the preheated concentrated solution is increased, and the concentrated solution enters a first-effect separator for flash evaporation so as to separate liquid drops in the water vapor from the steam to form secondary steam; the concentrated solution evaporated by the first stage forced evaporator enters a second stage forced evaporator for evaporation and enters a two-effect separator for flash evaporation so as to separate liquid drops in the water vapor from the steam to form secondary steam.
Further, secondary steam enters a compressor, an expansion tank is arranged in front of the compressor, namely the secondary steam respectively enters the outside of a heat exchange pipe of a first-stage forced evaporator and the outside of a heat exchange pipe of a second-stage forced evaporator to exchange heat with concentrated liquid in the corresponding heat exchange pipe, and latent heat released by the secondary steam is condensed into condensed water; and the condensed water is collected at the bottom of the heat exchange tube of the first-stage forced evaporator and the bottom of the heat exchange tube of the second-stage forced evaporator and then enters the first condensed water tank so as to be pumped into the two-stage plate preheater and then enters the second condensed water tank.
Further, after being concentrated, the concentrated solution in the first-stage forced evaporator automatically flows into the second-stage forced evaporator to be evaporated, and then enters a filter press for filter pressing and separation, so that centrifugal mother liquor and crystallized salt are generated.
Further, salt slurry at the bottom of the first-stage forced evaporator and at the bottom of the second-stage forced evaporator is conveyed to a centrifugal machine by a crystal slurry pump, namely salt centrifuged by the centrifugal machine is discharged, and concentrated solution centrifuged by the centrifugal machine is returned to the first-stage forced evaporator by a mother solution return pump to continue evaporation and crystallization.
Further, the filter mechanism includes: an RO water inlet tank; and a reverse osmosis membrane is arranged in the RO water inlet tank to filter the condensed water entering the RO water inlet tank from the second condensed water tank, namely the produced water is recycled to the first-stage forced evaporator and the second-stage forced evaporator after reaching the standard.
The utility model has the beneficial effects that the concentrated solution is pretreated by the pretreatment mechanism, high-boiling organic matter components (mainly humus which is difficult to degrade) in the inlet water of the concentrated solution can be removed, so that the high-efficiency separation of organic matter and salt is realized, the evaporation maintenance cost is reduced, the low-temperature MVR evaporation mechanism is adopted, the operation temperature is in the range of 55-70 ℃, the stable operation of evaporation can be ensured, the safety coefficient is properly reserved, the stable operation, the energy conservation and the environmental protection are realized, and the qualified discharge is ensured by filtering the condensed water by the filtering mechanism.
Additional features and advantages of the utility model 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 utility model.
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 description of the embodiments or 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 other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic block diagram of an MVR evaporation system for concentrate processing according to 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 clearly and completely described below with reference to the accompanying drawings, and it is apparent that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Fig. 1 is a schematic block diagram of an MVR evaporation system for concentrate processing according to the present invention.
In this embodiment, as shown in fig. 1, the present embodiment provides an MVR evaporation system for concentrate treatment, which includes: a pretreatment mechanism for pretreating the concentrated solution; the low-temperature MVR evaporation mechanism is used for carrying out low-temperature MVR evaporation on the pretreated concentrated solution to generate crystalline salt, mother liquor and condensed water; and the filtering mechanism is used for filtering the condensed water after the low-temperature MVR is evaporated so as to form clear liquid to be discharged.
In the embodiment, the high-concentration organic waste liquid generated by the pretreatment mechanism and the low-temperature MVR evaporation mechanism has high heat value, and can be sprayed back to a waste incineration plant for combustion-supporting power generation of a hearth, so that the problem of concentrated liquid is thoroughly solved; only a small part of residue is generated after the residue is treated by a low-temperature MVR evaporation mechanism, and dry residue generated after the residue is dehydrated through solid-liquid separation is collected and disposed; a small part of concentrated solution treated by the low-temperature MVR evaporation mechanism is transported to an incineration plant for treatment, and the accumulation of pollutants such as salt in the wastewater can be prevented.
In this embodiment, this embodiment is through pretreatment mechanism to the concentrate preliminary treatment, can get rid of concentrate influent medium high boiling point organic matter component (mainly be difficult degradation humus), thereby realize the high-efficient separation of organic matter and salinity, reduce the evaporation maintenance cost, and adopt low temperature MVR evaporation mechanism, operating temperature is in 55 ~70 ℃ within range, can guarantee the evaporation steady operation, suitably reserve factor of safety, realize the operation stable, energy-conservation and environmental protection, and filter the comdenstion water through filtering mechanism, guarantee qualified emission.
In this embodiment, the preprocessing mechanism includes: a feed tank and a material film at an inlet of the feed tank; the material membrane is suitable for filtering the concentrated solution entering the feeding tank to remove high-boiling-point organic matter components in the concentrated solution.
In this embodiment, the low temperature MVR evaporation mechanism includes: a feed pump, a two-stage plate preheater and an evaporation chamber; the feed pump is suitable for pumping the concentrated solution in the feed tank into the two-stage plate type preheater for preheating, namely the concentrated solution enters the evaporation chamber for two-stage concentration and evaporation after being preheated to be close to a bubble point so as to generate crystalline salt, concentrated mother liquor and condensed water.
In the embodiment, a first-stage forced evaporator and a second-stage forced evaporator are arranged in the evaporation chamber; the preheated concentrated solution enters a first-stage forced evaporator, the temperature of the preheated concentrated solution is increased, and the concentrated solution enters a first-effect separator for flash evaporation so as to separate liquid drops in the water vapor from the steam to form secondary steam; the concentrated solution evaporated by the first stage forced evaporator enters a second stage forced evaporator for evaporation and enters a two-effect separator for flash evaporation so as to separate liquid drops in the water vapor from the steam to form secondary steam.
In this embodiment, the secondary steam enters the compressor, and an expansion tank is configured in front of the compressor, that is, the secondary steam enters the outside of the heat exchange tube of the first-stage forced evaporator and the outside of the heat exchange tube of the second-stage forced evaporator respectively, exchanges heat with the concentrated solution in the corresponding heat exchange tube, and releases latent heat to be condensed into condensed water; and the condensed water is collected at the bottom of the heat exchange tube of the first-stage forced evaporator and the bottom of the heat exchange tube of the second-stage forced evaporator and then enters the first condensed water tank so as to be pumped into the two-stage plate preheater and then enters the second condensed water tank.
In the embodiment, the water in the concentrated solution is changed into water vapor to be evaporated and separated from the concentrated solution, and the concentrated solution is concentrated; the secondary steam generated in the evaporation process in the traditional evaporation process is condensed into condensed water by cooling water, the heat energy in the secondary steam is transferred into the cooling water and then diffused into the air, so that the heat energy waste and the cooling water consumption are caused, in the embodiment, the first stage forced evaporator and the second stage forced evaporator utilize corresponding compressors to compress the secondary steam generated by the first stage forced evaporator and the second stage forced evaporator so as to increase the pressure and the temperature of the secondary steam, then the heat source of the first stage forced evaporator and the second stage forced evaporator is used for replacing fresh steam, thereby realizing the reutilization of heat energy in secondary steam, recycling the heat energy of the first stage forced evaporator and the second stage forced evaporator, namely, as long as a small amount of electric power is provided to drive the compressor to work, the heat energy of the first-stage forced evaporator and the second-stage forced evaporator can be recycled and continuously evaporated without fresh steam; the compressor is not used for generating heat required by evaporation, but used for conveying the heat of the first-stage forced evaporator and the second-stage forced evaporator to form a heat cycle.
In this embodiment, the concentrated solution in the first stage forced evaporator is concentrated, and then enters the second stage forced evaporator by gravity flow to evaporate, and then enters the filter press to be filter-pressed and separated, so as to generate centrifugal mother liquor and crystallized salt.
In this embodiment, the salt slurry at the bottom of the first stage forced evaporator and the salt slurry at the bottom of the second stage forced evaporator are delivered to the centrifuge by the magma pump, i.e., the salt centrifuged by the centrifuge is discharged, and the concentrated solution centrifuged by the centrifuge is returned to the first stage forced evaporator by the mother liquor returning pump to continue evaporation and crystallization.
In the embodiment, the temperature of the concentrated solution is not less than 20 ℃, the concentrated solution is pumped to a two-stage plate preheater by a front process and enters a first-stage forced evaporator after being preheated, the temperature of the concentrated solution is raised by heat exchange between the concentrated solution in a heat exchange pipe of the first-stage forced evaporator and heating steam outside the heat exchange pipe, the concentrated solution enters a first-effect separator and then is flashed, and the first-effect separator separates and removes liquid drops in water vapor from the steam to form secondary steam; concentrated liquid in the first-stage forced evaporator is conveyed into a shell of the second-stage forced evaporator by a pump, the concentrated liquid in a heat exchange tube of the second-stage forced evaporator exchanges heat with shell steam to raise the temperature of raw materials, the raw materials enter a secondary-effect separator and then are subjected to flash evaporation, the secondary-effect separator separates liquid drops in water vapor from the steam to form secondary steam, the secondary steam in the primary-effect separator and the secondary-effect separator enters a compressor, an expansion tank is arranged in front of the compressor to prevent feed liquid from entering the compressor, the temperature and the pressure of the compressed water vapor are raised, the water vapor with higher temperature enters the outer side of the heat exchange tube of the first-stage forced evaporator and the outer side of the heat exchange tube of the second-stage forced evaporator to exchange heat with the concentrated liquid in the tube, and the water vapor is discharged and condensed into condensed water. Condensed water is collected at the bottoms of the heat exchange tubes of the first-stage forced evaporator and the second-stage forced evaporator and then enters a first condensed water tank, and is pumped into the two-stage plate preheater and then enters a second condensed water tank. After being concentrated, the concentrated solution in the first stage forced evaporator automatically flows into the second stage forced evaporator, then enters a filter press for separation, and the centrifugal mother solution is pumped back to the first stage forced evaporator and the second stage forced evaporator for evaporation.
In the embodiment, the first-stage forced evaporator adopts 1 compressor to compress the secondary steam, so that the temperature of the secondary steam is increased by 15 ℃ and the secondary steam is used as a heat source for evaporation; the second stage forced evaporator adopts 1 compressor and 1 Roots machine to compress the secondary steam, so that the temperature of the secondary steam is increased by 29 ℃ and the secondary steam is used as a heat source for evaporation; and water is sprayed at the outlet of the corresponding compressor, so that the overheat generated by the secondary steam passing through the compressor is eliminated.
The first-stage forced evaporator and the second-stage forced evaporator are started by adopting electric heating, and the corresponding compressor is started after the concentrated solution is heated to an evaporation state, so that the high efficiency and energy saving are realized.
In this example, a part of the concentrated mother liquor was incinerated (a small part of the concentrated mother liquor with a high organic content was less likely to evaporate crystalline salts).
In this embodiment, the filter mechanism includes: an RO water inlet tank; and a reverse osmosis membrane is arranged in the RO water inlet tank to filter the condensed water entering the RO water inlet tank from the second condensed water tank, namely the produced water is recycled to the first-stage forced evaporator and the second-stage forced evaporator after reaching the standard.
In conclusion, the concentrated solution is pretreated by the pretreatment mechanism, high-boiling-point organic matter components (mainly humus which is difficult to degrade) in inlet water of the concentrated solution can be removed, so that high-efficiency separation of organic matters and salt is realized, evaporation maintenance cost is reduced, a low-temperature MVR evaporation mechanism is adopted, the operation temperature is in the range of 55-70 ℃, stable operation of evaporation can be ensured, a safety coefficient is reserved properly, stable operation, energy conservation and environmental protection are realized, and qualified discharge is ensured by filtering condensed water by the filtering mechanism.
The components selected for use in the present application (components not illustrated for specific structures) are all common standard components or components known to those skilled in the art, and the structure and principle thereof can be known to those skilled in the art through technical manuals or through routine experimentation. Moreover, the software programs referred to in the present application are all prior art, and the present application does not relate to any improvement of the software programs.
In the description of the embodiments of the present invention, unless otherwise explicitly specified or limited, 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 meanings 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", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular 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 light of the foregoing description of the preferred embodiment of the present invention, many modifications and variations can be made by the worker in the light of the above teachings without departing from the spirit of the utility model. 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. An MVR evaporation system for concentrate processing, comprising:
a pretreatment mechanism for pretreating the concentrated solution;
the low-temperature MVR evaporation mechanism is used for carrying out low-temperature MVR evaporation on the pretreated concentrated solution to generate crystalline salt, mother liquor and condensed water;
the filtering mechanism is used for filtering the condensed water after the low-temperature MVR is evaporated so as to form clear liquid to be discharged;
the preprocessing mechanism comprises: a feed tank and a material film at an inlet of the feed tank;
the material membrane is suitable for filtering the concentrated solution entering the feeding tank to remove high-boiling-point organic matter components in the concentrated solution.
2. The MVR evaporation system for concentrate processing according to claim 1,
the low temperature MVR evaporation mechanism includes: a feed pump, a two-stage plate preheater and an evaporation chamber;
the feed pump is suitable for pumping the concentrated liquid in the feed tank into the two-stage plate-type preheater for preheating, namely
The concentrated solution enters an evaporation chamber for two-stage concentration and evaporation after being preheated to be close to a bubble point so as to generate crystalline salt, concentrated mother liquor and condensed water.
3. The MVR evaporation system for concentrate processing according to claim 2,
the evaporation chamber is internally provided with a first-stage forced evaporator and a second-stage forced evaporator;
the preheated concentrated solution enters a first-stage forced evaporator, the temperature of the preheated concentrated solution is increased, and the concentrated solution enters a first-effect separator for flash evaporation so as to separate liquid drops in the water vapor from the steam to form secondary steam;
the concentrated solution evaporated by the first stage forced evaporator enters a second stage forced evaporator for evaporation and enters a two-effect separator for flash evaporation so as to separate liquid drops in the water vapor from the steam to form secondary steam.
4. The MVR evaporation system for concentrate processing according to claim 3,
the secondary vapour entering the compressor and said compressor being preceded by an expansion tank, i.e.
The secondary steam enters the outside of the heat exchange tube of the first-stage forced evaporator and the outside of the heat exchange tube of the second-stage forced evaporator respectively to exchange heat with the concentrated solution in the corresponding heat exchange tube, and the latent heat released by the secondary steam is condensed into condensed water;
and the condensed water is collected at the bottom of the heat exchange tube of the first-stage forced evaporator and the bottom of the heat exchange tube of the second-stage forced evaporator and then enters the first condensed water tank so as to be pumped into the two-stage plate preheater and then enters the second condensed water tank.
5. The MVR evaporation system for concentrate processing according to claim 4,
after being concentrated, the concentrated solution in the first stage forced evaporator automatically flows into the second stage forced evaporator to be evaporated and then enters a filter press for filter pressing and separation so as to generate centrifugal mother liquor and crystallized salt.
6. The MVR evaporation system for concentrate processing according to claim 5,
the salt slurry at the bottom of the first stage forced evaporator and the salt slurry at the bottom of the second stage forced evaporator are conveyed to a centrifugal machine by a crystal slurry pump, namely
Discharging the salt after centrifugation by a centrifuge, and returning the concentrated solution after centrifugation by a mother liquor return pump to the first-stage forced evaporator for continuous evaporation and crystallization.
7. The MVR evaporation system for concentrate processing according to claim 4,
the filter mechanism includes: an RO water inlet tank;
the RO water inlet tank is provided with a reverse osmosis membrane to filter the condensed water entering the RO water inlet tank from the second condensed water tank, namely
And the produced water is recycled to the first-stage forced evaporator and the second-stage forced evaporator after reaching the standard.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121213312.2U CN216038723U (en) | 2021-06-01 | 2021-06-01 | MVR evaporation system for concentrated solution treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121213312.2U CN216038723U (en) | 2021-06-01 | 2021-06-01 | MVR evaporation system for concentrated solution treatment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216038723U true CN216038723U (en) | 2022-03-15 |
Family
ID=80614577
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202121213312.2U Active CN216038723U (en) | 2021-06-01 | 2021-06-01 | MVR evaporation system for concentrated solution treatment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216038723U (en) |
-
2021
- 2021-06-01 CN CN202121213312.2U patent/CN216038723U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN207525092U (en) | A kind of garbage percolation liquid treating system and refuse disposal system | |
| US12030801B2 (en) | Saline wastewater treatment system using solar-assisted heat pump | |
| CN203591603U (en) | Sextuple-effect evaporator | |
| CN112624475A (en) | Zero-discharge treatment system and process for landfill leachate | |
| CN104628065A (en) | Chemical pharmaceutical wastewater treatment system and method | |
| CN113735209A (en) | Full-quantification landfill leachate treatment device and process | |
| CN113307433A (en) | Four-effect cross-flow pharmaceutical wastewater evaporative crystallization system with external heat exchanger | |
| CN216038723U (en) | MVR evaporation system for concentrated solution treatment | |
| CN113277665A (en) | Method and device for treating high-concentration high-salinity wastewater through electrolytic evaporation | |
| CN113082749A (en) | Treatment method and system for evaporation crystallization and secondary steam purification of fly ash water washing liquid | |
| WO2018045709A1 (en) | Power plant seawater desalination treatment device and method | |
| CN210313974U (en) | Sludge reduction treatment system | |
| CN219174370U (en) | Concentrated vaporization system of membrane dense water | |
| CN115676973B (en) | High-concentration complex wastewater treatment and resource recovery system and working method thereof | |
| CN216472686U (en) | Epoxy waste water treatment equipment | |
| CN113354009A (en) | MVR evaporation process for treating concentrated solution | |
| CN106186201A (en) | A kind of device and method of water-electricity cogeneration | |
| CN206108988U (en) | Utilize water treatment facilities of power plant's waste heat | |
| CN113526824A (en) | Heat energy and solar energy linkage drying sludge treatment equipment and process | |
| CN204684697U (en) | The innocuity disposal system of a kind of changing food waste natural pond liquid | |
| CN210645170U (en) | Double-effect external circulation evaporator | |
| CN111517547A (en) | Converter valve cooling tower wastewater treatment system and treatment process | |
| CN212610078U (en) | Converter valve cooling tower effluent disposal system | |
| CN112661215A (en) | Treatment process and system for landfill leachate membrane concentrated solution | |
| CN106186127B (en) | Thermal evaporation concentration device for treating membrane concentrated solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |