CN217287198U - MVR evaporation concentration system - Google Patents
MVR evaporation concentration system Download PDFInfo
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- CN217287198U CN217287198U CN202220239928.5U CN202220239928U CN217287198U CN 217287198 U CN217287198 U CN 217287198U CN 202220239928 U CN202220239928 U CN 202220239928U CN 217287198 U CN217287198 U CN 217287198U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The embodiment of the utility model discloses an MVR evaporation concentration system, which comprises a first evaporator, a second evaporator, a gas washing tower and a supercharging mechanism, wherein the liquid outlet end of the concentrated solution of the first evaporator is connected with the liquid inlet end of the second evaporator, the gas outlet ends of the first evaporator and the second evaporator enter the supercharging mechanism through the gas washing tower, the compression gas outlet ends of the supercharging mechanism are respectively connected with the gas inlet ends of the first evaporator and the second evaporator, the condensate outlets of the first evaporator and the second evaporator are respectively connected with a condensate tank, the liquid outlet end of the second evaporator is connected with a liquid storage tank, the supercharging mechanism is a three-level compression structure and comprises a first compressor, a second compressor and a third compressor which are connected in series, the system adopts evaporation type heat exchange, and can be combined with multi-level compressed gas to reach the system again, thereby reducing energy waste, and improving the reliability of stable operation of equipment by using the system, the reasonable proportion of the secondary steam distribution can reduce the whole equipment investment and the operation cost.
Description
Technical Field
The embodiment of the utility model provides a relate to and mix concentrated technical field of liquid, concretely relates to MVR evaporative concentration system.
Background
The fly ash refers to a large amount of fly ash generated in the process of burning household garbage to generate electricity, the fly ash has great toxicity hazard, and the fly ash contains inorganic heavy metals with strong toxicity and most toxic organic dioxin. Once the waste incineration fly ash containing heavy metals and dioxin enters a common waste landfill disorderly, the waste incineration fly ash is a disaster to people around the waste landfill, so that the traditional waste treatment mode mainly based on sanitary landfill needs to be changed so as to avoid the waste of a large amount of land resources and the occurrence of huge environmental pollution events. Therefore, the resource utilization of fly ash is more and more highly regarded by the nation.
The fly ash washing refers to mixing and uniformly stirring fly ash and water, and then carrying out solid-liquid separation on the fly ash washing slurry. The fly ash water washing liquid refers to liquid generated after washing and solid-liquid separation of fly ash. The heavy metal and calcium and magnesium ions in the water are removed from the washing liquid generated in the fly ash washing pretreatment process through water treatment processes such as physical sedimentation, flocculation precipitation, chemical reaction, pH adjustment, multi-stage filtration and the like. The fly ash washing liquid after hardness removal generates high-salinity wastewater, and the main components of the fly ash washing liquid are NaCl, KCl and other trace impurities. The generated high-salt water washing liquid can not meet the standard of direct discharge, and the crystallization separation of industrial salt and the standard-reaching discharge or recycling of water are realized after the treatment.
The Mechanical Vapor Recompression (MVR) technology is an efficient evaporation energy-saving method, the technology replaces raw steam with electric energy consumed by a compressor, the pressure and the temperature of secondary steam are improved, the latent heat and the enthalpy value of the secondary steam in the evaporation process are recycled, the cyclic utilization of the self energy is realized, and the energy consumption in the evaporation concentration process is reduced. The evaporation and concentration of the fly ash water washing liquid by utilizing the MVR technology can realize the resource recovery of potassium and sodium salt and the cyclic utilization of condensed water. In the existing concentration system, most of the heat exchangers are adopted, heat exchange concentration is realized, although the purpose of concentrating mixed liquid can be realized by the method, in the using process, the heat exchangers which are recycled need to continuously supply heat through heat sources, the problem of heat source waste exists after circulation, meanwhile, the heat exchange process needs to be repeated, and the concentration efficiency is low.
SUMMERY OF THE UTILITY MODEL
Therefore, the embodiment of the utility model provides a MVR evaporation concentration system to among the solution prior art because the concentrated system of heat exchanger formula, the heat exchanger need constantly supply the heat source and the heat transfer structure is complicated and the energy that leads to is extravagant and concentrated inefficiency, the high problem of maintenance cost.
In order to achieve the above object, the embodiments of the present invention provide the following technical solutions:
the utility model discloses an in the first aspect of embodiment, provide a MVR evaporative concentration system, including first evaporimeter, second evaporimeter, scrubbing tower and booster mechanism, the concentrate of first evaporimeter goes out the liquid end and connects the feed liquor end of second evaporimeter, the end of giving vent to anger of first evaporimeter and second evaporimeter all gets into booster mechanism through the scrubbing tower, booster mechanism's compression is given vent to anger and is held and connect respectively the end of admitting air of first evaporimeter and second evaporimeter, condensate tank is all connected in the condensate export of first evaporimeter and second evaporimeter, the liquid storage pot is connected to the play liquid end of second evaporimeter, booster mechanism is tertiary compression structure, including first compressor, second compressor and the third compressor of establishing ties.
Furthermore, the air outlet end of the gas washing tower is sequentially connected with a first compressor, a second compressor and a third compressor, and the compression air outlet end of the third compressor is respectively connected with the air inlet ends of the first evaporator and the second evaporator.
In another embodiment of the present invention, the gas outlet end of the scrubber is connected to the first compressor, the second compressor and the third compressor in sequence, the gas outlet end of the second compressor is connected to the gas inlet end of the third compressor and the gas inlet end of the first evaporator respectively, and the gas outlet end of the third compressor is connected to the gas inlet end of the second evaporator.
According to the utility model discloses an embodiment has following advantage: the system adopts heat exchange and combines multi-stage compressed gas to reach the system again, thereby reducing energy waste, recycling gas repeatedly, improving concentration efficiency, facilitating maintenance of a distributed heat exchange structure and reducing maintenance cost, the multistage combination form of the compressors in the MVR evaporation technology can efficiently match the air passing amount and the temperature rise of a single compressor, the investment and the operation cost are reduced, the reliability of stable operation of equipment can be improved by using the system, and the overall equipment investment and the operation cost can be reduced by reasonably distributing the proportion of secondary steam.
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. It should be apparent that the drawings in the following description are merely exemplary, and that other embodiments can be derived from the drawings provided by those of ordinary skill in the art without inventive effort.
The structure, proportion, size and the like shown in the present specification are only used for matching with the content disclosed in the specification, so as to be known and read by people familiar with the technology, and are not used for limiting the limit conditions which can be implemented by the present invention, so that the present invention has no technical essential significance, and the modification of any structure, the change of proportion relation or the adjustment of size all fall within the scope which can be covered by the technical content disclosed by the present invention without affecting the efficacy and the purpose which can be achieved by the present invention.
Fig. 1 is a schematic structural diagram of an MVR evaporation and concentration system according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of an MVR evaporation and concentration system according to another embodiment of the present invention.
In the figure: 1. a first evaporator; 2. a second evaporator; 3. a scrubber tower; 4. a pressurization mechanism; 4-1, a first compressor; 4-2, a second compressor; 4-3 and a third compressor.
Detailed Description
The present invention is described in terms of specific embodiments, and other advantages and benefits of the present invention will become apparent to those skilled in the art from the following disclosure. 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.
In the present specification, the terms "upper", "lower", "left", "right", "middle", and the like are used for the sake of clarity only, and are not intended to limit the scope of the present invention, and changes or adjustments of the relative relationship thereof are also considered to be the scope of the present invention without substantial changes in the technical content.
As shown in fig. 1, it shows the MVR evaporation concentration system that the embodiment of the present invention provides, it is the first embodiment of this system, including first evaporator 1, second evaporator 2, gas washing tower 3 and booster mechanism 4, the feed liquor end of second evaporator 2 is connected to the concentrate liquid end of first evaporator 1, the end of giving vent to anger of first evaporator 1 and second evaporator 2 all gets into mechanism 4 through gas washing tower 3, the end of giving vent to anger of booster mechanism 4 is connected the feed liquor end of first evaporator 1 and second evaporator 2 respectively, the condensate liquid tank is all connected in the condensate export of first evaporator 1 and second evaporator 2, the liquid storage pot is connected to the liquid end of second evaporator 2, booster mechanism 4 is the tertiary compression structure, booster mechanism 4-1, second compressor 4-2 and third compressor 4-3 including establishing ties.
The system adopts evaporation type heat exchange, and meanwhile, multi-stage compressed gas is combined to arrive in the system again, so that energy waste is reduced, the gas is recycled, the concentration efficiency is improved, the distributed heat exchange structure is easy to maintain, the maintenance cost is reduced, the multi-stage combination form of the compressors in the MVR evaporation technology can efficiently match the air passing amount and the temperature rise of a single compressor, the investment and the operating cost are reduced, the reliability of stable operation of equipment can be improved by using the system, and the investment and the operating cost of the whole equipment are reduced.
The air outlet end of the gas washing tower 3 is sequentially connected with a pressurization mechanism 4-1, a second compressor 4-2 and a third compressor 4-3, and the compressed air outlet end of the third compressor 4-3 is respectively connected with the air inlet ends of the first evaporator 1 and the second evaporator 2.
In the embodiment, the three groups of compressors are arranged in series end to end, the gas in the first evaporator 1 and the gas in the second evaporator 2 are all subjected to gas washing through the gas washing tower 3 and then are compressed step by step to be heated and returned to the first evaporator 1 and the second evaporator 2, the evaporation efficiency is improved, secondary steam is fully utilized, and the embodiment is effectively applied to evaporation and concentration of materials with the water content of more than 40%.
As shown in fig. 2, a second embodiment of the scheme includes a first evaporator 1, a second evaporator 2, a gas washing tower 3 and a pressurization mechanism 4, a liquid outlet end of a concentrated solution of the first evaporator 1 is connected with a liquid inlet end of the second evaporator 2, gas outlet ends of the first evaporator 1 and the second evaporator 2 enter the pressurization mechanism 4 through the gas washing tower 3, a compressed gas outlet end of the pressurization mechanism 4 is respectively connected with a gas inlet end of the first evaporator 1 and a gas inlet end of the second evaporator 2, condensate outlets of the first evaporator 1 and the second evaporator 2 are respectively connected with a condensate tank, a liquid outlet end of the second evaporator 2 is connected with a liquid storage tank, and the pressurization mechanism 4 is a three-stage compression structure and includes a pressurization mechanism 4-1, a second compressor 4-2 and a third compressor 4-3 which are connected in series.
The air outlet end of the gas washing tower 3 is sequentially connected with a pressurization mechanism 4-1, a second compressor 4-2 and a third compressor 4-3, the air outlet end of the second compressor 4-2 is respectively connected with the air inlet end of the third compressor 4-3 and the air inlet end of the first evaporator 1, and the compressed air outlet end of the third compressor 4-3 is connected with the air inlet end of the second evaporator 2.
In this embodiment, according to the evaporation efficiency of the first evaporator 1 and the second evaporator 2 and the water content of the evaporation material, optionally, the gas of the two evaporators sequentially enters the pressurization mechanism 4-1 and the second compressor 4-2 to be compressed and heated, the high-temperature steam enters the third compressor 4-3 and the first evaporator 1 respectively, and the high-temperature steam of the third compressor 4-3 enters the second evaporator 2 again, wherein the secondary steam entering the third-stage compressor accounts for 40% -60% of the total secondary steam, and the high-efficiency evaporation of the first evaporator 1 and the second evaporator 2 can be matched through the form of the branched compressed high-temperature steam, so that the evaporation efficiency can be improved to the maximum efficiency, and this embodiment is effective for the evaporation and concentration of the material with the water content below 40%.
In the above two embodiments, each of the first evaporator 1 and the second evaporator 2 is provided with a preheater (not shown), which may be a temperature raising device such as an electric heater.
When the system is used, firstly, a preheater is adopted for first temperature rise evaporation, raw material liquid is evaporated and concentrated through a first evaporator 1, concentrated liquid enters a second evaporator 2, and concentrated liquid subjected to secondary evaporation and concentration is discharged out of the system to be treated in the next procedure; the working state of the evaporator is the internal range micro negative pressure (0.075 Mpa).
The secondary steam (92 ℃) generated by the first evaporator 1 and the second evaporator 2 is merged into the gas washing tower 3, enters the first evaporator 1 after being washed by the gas washing tower 3, the secondary steam in the supercharging mechanism 4-1 is compressed, heated and boosted to improve the enthalpy value, the saturated steam with the improved enthalpy enters the second compressor 4-2 to be continuously compressed to improve the enthalpy value, then part of the high-temperature steam directly enters the first evaporator 1 to be used as a heating heat source, part of the (108 ℃) high-temperature steam continuously enters the third compressor 4-3 to be compressed to be used as a heating heat source of the second evaporator 2, and the secondary steam generated by the evaporators is recycled, so that the cyclic utilization of the evaporated gas is ensured, the energy waste is reduced, and the efficiency is improved.
In the embodiment of the scheme, the total temperature rise of the first-stage compressor and the second-stage compressor is controlled to be between 15 and 18 ℃, the pressure ratio of the third-stage compressor is controlled to be between 1.2 and 1.4, high-temperature steam is condensed as condensate after exchanging heat with an evaporator to preheat a raw material liquid or collect the raw material liquid, and compared with the existing concentration system, the implementation of the system enables the investment ratio of the whole equipment to be reduced by about 2.1 to 4.3 percent.
Although the invention has been described in detail with respect to the general description and the specific embodiments, it will be apparent to those skilled in the art that modifications and improvements can be made based on the invention. Therefore, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (4)
1. The utility model provides a MVR evaporative concentration system, includes first evaporimeter, second evaporimeter, scrubbing tower and booster mechanism, its characterized in that, the feed liquor end of second evaporimeter is connected to the concentrate liquid end of first evaporimeter, the end of giving vent to anger of first evaporimeter and second evaporimeter all gets into booster mechanism through the scrubbing tower, booster mechanism's compression is given vent to anger the end and is connected respectively the inlet end of first evaporimeter and second evaporimeter, the condensate tank is all connected with the condensate export of second evaporimeter to first evaporimeter, the liquid storage pot is connected to the play liquid end of second evaporimeter, booster mechanism is tertiary compression structure, including first compressor, second compressor and the third compressor of establishing ties.
2. The MVR evaporation concentration system according to claim 1, wherein the gas outlet end of the gas washing tower is sequentially connected with a first compressor, a second compressor and a third compressor, and the compressed gas outlet end of the third compressor is respectively connected with the gas inlet ends of the first evaporator and the second evaporator.
3. The MVR evaporation and concentration system according to claim 1, wherein the gas outlet end of the gas washing tower is sequentially connected with a first compressor, a second compressor and a third compressor, the gas outlet end of the second compressor is respectively connected with the gas inlet end of the third compressor and the gas inlet end of the first evaporator, and the compressed gas outlet end of the third compressor is connected with the gas inlet end of the second evaporator.
4. The MVR evaporative concentration system of claim 1, wherein a preheater is provided inside each of the first evaporator and the second evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202220239928.5U CN217287198U (en) | 2022-01-28 | 2022-01-28 | MVR evaporation concentration system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220239928.5U CN217287198U (en) | 2022-01-28 | 2022-01-28 | MVR evaporation concentration system |
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| CN217287198U true CN217287198U (en) | 2022-08-26 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT17768U3 (en) * | 2022-09-27 | 2023-03-15 | Gig Karasek Gmbh | Plant and process for the concentration of substance-containing liquids by multi-stage evaporation |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT17768U3 (en) * | 2022-09-27 | 2023-03-15 | Gig Karasek Gmbh | Plant and process for the concentration of substance-containing liquids by multi-stage evaporation |
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