CN214512728U - Multi-set MVR evaporation cooperative system - Google Patents
Multi-set MVR evaporation cooperative system Download PDFInfo
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- CN214512728U CN214512728U CN202023081607.7U CN202023081607U CN214512728U CN 214512728 U CN214512728 U CN 214512728U CN 202023081607 U CN202023081607 U CN 202023081607U CN 214512728 U CN214512728 U CN 214512728U
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Abstract
The utility model provides a many sets of MVR evaporation cooperative system, including first separation chamber, first heating chamber, first vapor compressor, first circulating pump, first distilled water pump, second separation chamber, second heating chamber, second vapor compressor, second circulating pump and second distilled water pump, first circulating pump export and second separation chamber bottom intercommunication, second circulating pump export and first separation chamber bottom intercommunication, first distilled water pump export and second separation chamber bottom intercommunication, second distilled water pump export and first separation chamber bottom intercommunication. This many sets of MVR evaporation cooperative system can shorten MVR evaporation system boot time greatly, also makes the operation cost very reduce.
Description
Technical Field
The utility model relates to a landfill leachate treatment technology especially relates to a many sets of MVR evaporation cooperative system.
Background
With the increase of the number of cities and population in China, the urban garbage also increases sharply. According to statistics, the annual production waste reaches 1.5 hundred million tons, and the average production waste is increased at a speed of 9%/year, wherein 70 hundred million tons of untreated waste accounts for 8.3% of the total land in China. The discharge of solid waste is expected to occupy 85% of land in the next 20 years, and the serious garbage pollution problem exists in most regions of the country. Most urban solid garbage in China adopts three types of composting, landfill or incineration, wherein the landfill is the main treatment mode in China. In the process of landfill stacking, waste water with high-concentration organic matters or inorganic matters is generated under the action of various external factors such as extrusion and the like, and is called landfill leachate. The water quality has wide variation range, and the organic pollutants have various types and high concentration and contain various carcinogens, auxiliary carcinogens, carcinogens and metal ions. When the garbage leachate permeates into underground water and surface water, the quality of the surface water is polluted, the underground water loses use value, and direct influence is caused on human health and industrial and agricultural water sources. Because the components of the landfill leachate are complex, the landfill leachate has higher toxicity, high COD value and high ammonia nitrogen content, and the treatment difficulty of the landfill leachate is very high.
At present, the MVR evaporation system has good effect in the treatment of landfill leachate, and a gas washing system matched with the rear end of the MVR evaporation system has good effect in COD and ammonia nitrogen treatment. Before the MVR evaporation system starts to operate, the time for the MVR evaporation system to heat to reach the normal continuous operation temperature is long, the heat required in the heating process is more, and a large amount of high-temperature circulating liquid is discharged when the MVR evaporation system is stopped. The following disadvantages exist in the specific application process: when the MVR evaporation system is shut down, a large amount of high-temperature circulating liquid in the equipment needs to be emptied, so that a large amount of energy loss is caused; when the MVR evaporation system is started to heat up, a large amount of raw steam is needed to heat the equipment and the circulating liquid in the equipment, and the starting to heat up and heating time is long (generally about 24 hours).
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a many sets of MVR evaporation cooperative system to the problem that a large amount of energy intensification heating and time are longer that many sets of MVR evaporation system start need consume of evacuation high temperature circulation liquid can cause a large amount of energy loss, MVR evaporation system when shutting down at present, this system can shorten MVR evaporation system start time greatly, does and makes the operation cost very reduce.
In order to achieve the above object, the utility model adopts the following technical scheme: a multi-set MVR evaporation cooperative system comprises a first separation chamber, a first heating chamber, a first vapor compressor, a first circulating pump, a first distilled water pump, a second separation chamber, a second heating chamber, a second vapor compressor, a second circulating pump and a second distilled water pump,
the first separation chamber bottom circulating liquid outlet is communicated with a first heating chamber cold side inlet through a first circulating pump, and the first heating chamber cold side outlet is communicated with a first separation chamber circulating liquid inlet; the steam outlet of the first separation chamber is communicated with the inlet of a first steam compressor, and the outlet of the first steam compressor is communicated with the hot side inlet of the first heating chamber; the non-condensable gas outlet of the first heating chamber is communicated with an emptying pipeline; the condensed water outlet of the first heating chamber is communicated with the subsequent section through a first distilled water pump;
the circulating liquid outlet at the bottom of the second separation chamber is communicated with the cold side inlet of the second heating chamber through a second circulating pump, and the cold side outlet of the second heating chamber is communicated with the circulating liquid inlet of the second separation chamber; the steam outlet of the second separation chamber is communicated with the inlet of a second steam compressor, and the outlet of the second steam compressor is communicated with the hot side inlet of the second heating chamber; the noncondensable gas outlet of the second heating chamber is communicated with an emptying pipeline; the condensed water outlet of the second heating chamber is communicated with the subsequent section through a second distilled water pump;
the outlet of the first circulating pump is communicated with the bottom of the second separation chamber, the outlet of the second circulating pump is communicated with the bottom of the first separation chamber, the outlet of the first distilled water pump is communicated with the bottom of the second separation chamber, and the outlet of the second distilled water pump is communicated with the bottom of the first separation chamber.
Further, the first heating chamber and the second heating chamber are both tube type heat exchangers.
Furthermore, the first heating chamber and the second heating chamber have the same specification.
Further, the non-condensable gas outlets of the first heating chamber and the second heating chamber are converged into a pipeline. When one set of MVR evaporation system is started to heat up, high-temperature non-condensable gas in the non-condensable gas main pipe can be used for heating the equipment and circulating liquid of the equipment. The process design not only reduces the loss of energy, but also greatly reduces the startup time of the MVR evaporation system.
The utility model discloses the operating principle of evaporating system noncondensable gas recovery system: concentrated solution generated by the first separation chamber 1 is conveyed to the first heating chamber 2 through the first circulating pump 4, heated to an overheated state through high-temperature steam in the shell pass of the first heating chamber 2, and returned to the first separation chamber 1 (corresponding to the pipeline I). Because the pressure in the first separation chamber 1 is small, the material in an overheated state is subjected to flash evaporation, and secondary steam generated by flash evaporation returns to the shell pass of the first heating chamber 2 through the second steam compressor 3 to continuously exchange heat with the low-temperature material (corresponding to the pipeline II). The noncondensable gas in the shell pass of the first heating chamber 2 is collected and then is emptied (corresponding to a pipeline III), and the condensed water after the heat exchange of the high-temperature steam in the shell pass of the first heating chamber 2 is conveyed to a subsequent working section (corresponding to a pipeline IV) through a first distilled water pump 5.
The concentrated solution generated by the second separation chamber 6 is delivered to the second heating chamber 7 through the second circulating pump 9, heated to an overheated state by high-temperature steam in the shell pass of the second heating chamber 7, and returned to the second separation chamber 6 (corresponding to the pipeline I). Because the pressure in the second separation chamber 6 is small, the material in an overheated state is subjected to flash evaporation, and secondary steam generated by flash evaporation returns to the shell pass of the second heating chamber 7 through the second steam compressor 8 to continuously exchange heat with the low-temperature material (corresponding to the pipeline II). The non-condensable gas in the shell pass of the second heating chamber 7 is collected and then emptied (corresponding to a pipeline III), and condensed water after heat exchange of high-temperature steam in the shell pass of the second heating chamber 7 is conveyed to a subsequent working section (corresponding to a pipeline IV) through a second distilled water pump 10;
the liquid in line i (recycle/concentrate) can be fed to the second separation chamber 6 by means of the first circulation pump 4. The liquid in line i (recycle/concentrate) can be fed to the first separation chamber 1 by means of a second circulation pump 9. The liquid (distilled water) in line iv can be brought into the second separation chamber 6 by means of the first distilled water pump 5. The liquid (distilled water) in the line iv can be introduced into the first separation chamber 1 by means of the second distilled water pump 10.
The utility model discloses many sets of MVR evaporation cooperative system has shortened MVR evaporation system start time greatly, can also greatly reduce the operation cost, compares with prior art and has following advantage:
1) the utility model discloses design a set of noncondensable gas pipeline to the equipment heating between pipeline, the many sets of MVR vaporization systems of a set of circulation liquid evacuation in the cooperation of many sets of MVR vaporization.
2) The utility model discloses start reduction energy loss's circulation liquid pipeline design with higher speed between many sets of MVR evaporation cooperative system, high temperature circulation liquid can be recycle each other.
3) The utility model discloses the concentrated liquid pipeline design of start with higher speed between many sets of MVR evaporation cooperative system, high temperature concentrate can the mutual utilization.
4) The utility model discloses the distilled water pipeline design of starting up with higher speed between many sets of MVR evaporation cooperative system, high temperature distilled water can the mutual utilization.
5) The utility model discloses start with higher speed between many sets of MVR evaporation cooperative system and reduce energy loss's noncondensable gas piping design, high temperature noncondensable gas can the utilization each other.
To sum up, the utility model discloses in high temperature circulation liquid, high temperature concentrate, high temperature distilled water and the noncondensable gas of high temperature between many sets of MVR evaporation cooperative system can get into each set of MVR evaporating system respectively, can make energy recuperation can accelerate the process design of MVR evaporating system start again. The utility model discloses the process design of many sets of MVR evaporation cooperative system start has fully played many sets of MVR evaporation system's synergism, can shorten MVR evaporation system start time greatly, does and makes the operation cost very reduce.
Drawings
FIG. 1 is a schematic diagram of a multi-set MVR evaporation synergy system.
Detailed Description
The invention is further illustrated below with reference to the following examples:
example 1
The embodiment discloses a multi-set MVR evaporation cooperative system, which comprises a first separation chamber 1, a first heating chamber 2, a first vapor compressor 3, a first circulating pump 4, a first distilled water pump 5, a second separation chamber 6, a second heating chamber 7, a second vapor compressor 8, a second circulating pump 9 and a second distilled water pump 10,
the bottom circulating liquid outlet of the first separation chamber 1 is communicated with the cold side inlet of the first heating chamber 2 through a first circulating pump 4, and the cold side outlet of the first heating chamber 2 is communicated with the circulating liquid inlet of the first separation chamber 1; the steam outlet of the first separation chamber 1 is communicated with the inlet of a first steam compressor 3, and the outlet of the first steam compressor 3 is communicated with the hot side inlet of the first heating chamber 2; the non-condensable gas outlet of the first heating chamber 2 is communicated with an emptying pipeline; a condensed water outlet of the first heating chamber 2 is communicated with a subsequent section through a first distilled water pump 5;
the circulating liquid outlet at the bottom of the second separation chamber 6 is communicated with the cold side inlet of the second heating chamber 7 through a second circulating pump 9, and the cold side outlet of the second heating chamber 7 is communicated with the circulating liquid inlet of the second separation chamber 6; the steam outlet of the second separation chamber 6 is communicated with the inlet of a second steam compressor 8, and the outlet of the second steam compressor 8 is communicated with the hot side inlet of the second heating chamber 7; the non-condensable gas outlet of the second heating chamber 7 is communicated with an emptying pipeline; a condensed water outlet of the second heating chamber 7 is communicated with a subsequent section through a second distilled water pump 10;
the outlet of the first circulating pump 4 is communicated with the bottom of the second separating chamber 6, the outlet of the second circulating pump 9 is communicated with the bottom of the first separating chamber 1, the outlet of the first distilled water pump 5 is communicated with the bottom of the second separating chamber 6, and the outlet of the second distilled water pump 10 is communicated with the bottom of the first separating chamber 1.
The first heating chamber 2 and the second heating chamber 7 are both tube type heat exchangers. The first heating chamber 2 and the second heating chamber 7 are of the same size. The non-condensable gas outlets of the first heating chamber 2 and the second heating chamber 7 are converged into a pipeline. When one set of MVR evaporation system is started to heat up, high-temperature non-condensable gas in the non-condensable gas main pipe can be used for heating the equipment and circulating liquid of the equipment. The process design not only reduces the loss of energy, but also greatly reduces the startup time of the MVR evaporation system.
The utility model discloses the operating principle of evaporating system noncondensable gas recovery system: concentrated solution generated by the first separation chamber 1 is conveyed to the first heating chamber 2 through the first circulating pump 4, heated to an overheated state through high-temperature steam in the shell pass of the first heating chamber 2, and returned to the first separation chamber 1 (corresponding to the pipeline I). Because the pressure in the first separation chamber 1 is small, the material in an overheated state is subjected to flash evaporation, and secondary steam generated by flash evaporation returns to the shell pass of the first heating chamber 2 through the second steam compressor 3 to continuously exchange heat with the low-temperature material (corresponding to the pipeline II). The noncondensable gas in the shell pass of the first heating chamber 2 is collected and then is emptied (corresponding to a pipeline III), and the condensed water after the heat exchange of the high-temperature steam in the shell pass of the first heating chamber 2 is conveyed to a subsequent working section (corresponding to a pipeline IV) through a first distilled water pump 5.
The concentrated solution generated by the second separation chamber 6 is delivered to the second heating chamber 7 through the second circulating pump 9, heated to an overheated state by high-temperature steam in the shell pass of the second heating chamber 7, and returned to the second separation chamber 6 (corresponding to the pipeline I). Because the pressure in the second separation chamber 6 is small, the material in an overheated state is subjected to flash evaporation, and secondary steam generated by flash evaporation returns to the shell pass of the second heating chamber 7 through the second steam compressor 8 to continuously exchange heat with the low-temperature material (corresponding to the pipeline II). The non-condensable gas in the shell pass of the second heating chamber 7 is collected and then emptied (corresponding to a pipeline III), and condensed water after heat exchange of high-temperature steam in the shell pass of the second heating chamber 7 is conveyed to a subsequent working section (corresponding to a pipeline IV) through a second distilled water pump 10;
as shown in figure 1, when one set of MVR evaporation system is shut down, a large amount of high-temperature circulating liquid (pipeline I) can be emptied to the other set of MVR evaporation system which needs to be started. The process design not only avoids energy loss, but also reduces the energy consumption required by the equipment when the equipment is heated.
As shown in fig. 1, when one set of MVR evaporation system needs to be started, the other set of running MVR evaporation system can make the high-temperature concentrated solution (pipeline i) enter the MVR evaporation system needing to be started by increasing the rotation speed of the compressor. The process design does not affect the operation of the MVR evaporation system and greatly accelerates the starting time of another set of MVR evaporation system.
As shown in fig. 1, when one set of MVR evaporation system needs to be started up with clean water, the other set of MVR evaporation system in operation can make a part of high-temperature distilled water (pipeline iv) enter the MVR evaporation system needing to be started up by increasing the rotation speed of the compressor. The process design does not influence the operation of the MVR evaporation system, and greatly shortens the starting time of the other set of MVR evaporation system.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (4)
1. A multi-set MVR evaporation cooperative system is characterized by comprising a first separation chamber (1), a first heating chamber (2), a first vapor compressor (3), a first circulating pump (4), a first distilled water pump (5), a second separation chamber (6), a second heating chamber (7), a second vapor compressor (8), a second circulating pump (9) and a second distilled water pump (10);
the bottom circulating liquid outlet of the first separation chamber (1) is communicated with the cold side inlet of the first heating chamber (2) through a first circulating pump (4), and the cold side outlet of the first heating chamber (2) is communicated with the circulating liquid inlet of the first separation chamber (1); the steam outlet of the first separation chamber (1) is communicated with the inlet of a first steam compressor (3), and the outlet of the first steam compressor (3) is communicated with the hot side inlet of the first heating chamber (2); the non-condensable gas outlet of the first heating chamber (2) is communicated with an emptying pipeline; a condensed water outlet of the first heating chamber (2) is communicated with a subsequent section through a first distilled water pump (5);
the bottom circulating liquid outlet of the second separation chamber (6) is communicated with the cold side inlet of the second heating chamber (7) through a second circulating pump (9), and the cold side outlet of the second heating chamber (7) is communicated with the circulating liquid inlet of the second separation chamber (6); the steam outlet of the second separation chamber (6) is communicated with the inlet of a second steam compressor (8), and the outlet of the second steam compressor (8) is communicated with the hot side inlet of a second heating chamber (7); the non-condensable gas outlet of the second heating chamber (7) is communicated with an emptying pipeline; a condensed water outlet of the second heating chamber (7) is communicated with a subsequent section through a second distilled water pump (10);
the outlet of the first circulating pump (4) is communicated with the bottom of the second separating chamber (6), the outlet of the second circulating pump (9) is communicated with the bottom of the first separating chamber (1), the outlet of the first distilled water pump (5) is communicated with the bottom of the second separating chamber (6), and the outlet of the second distilled water pump (10) is communicated with the bottom of the first separating chamber (1).
2. The multiple MVR evaporation synergy system according to claim 1, wherein the first heating chamber (2) and the second heating chamber (7) are both tube type heat exchangers.
3. The MVR evaporative coordination system according to claim 1, wherein the first heating chamber (2) and the second heating chamber (7) are of the same size.
4. The multiple MVR evaporation synergy system according to claim 1, wherein the non-condensable gas outlets of the first heating chamber (2) and the second heating chamber (7) are combined into a single pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023081607.7U CN214512728U (en) | 2020-12-21 | 2020-12-21 | Multi-set MVR evaporation cooperative system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202023081607.7U CN214512728U (en) | 2020-12-21 | 2020-12-21 | Multi-set MVR evaporation cooperative system |
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| CN214512728U true CN214512728U (en) | 2021-10-29 |
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