CN214512794U - Non-condensable gas recovery system of evaporation system - Google Patents
Non-condensable gas recovery system of evaporation system Download PDFInfo
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- CN214512794U CN214512794U CN202023082089.0U CN202023082089U CN214512794U CN 214512794 U CN214512794 U CN 214512794U CN 202023082089 U CN202023082089 U CN 202023082089U CN 214512794 U CN214512794 U CN 214512794U
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Abstract
The utility model provides an evaporating system noncondensable gas recovery system, including first separation chamber, first circulating pump, first heating chamber, first distilled water jar, first distilled water pump, first vapor compressor, second separation chamber, second circulating pump, second heating chamber, second distilled water jar, second distilled water pump and second vapor compressor. The utility model discloses still disclose the technology is retrieved to the non-condensable gas of evaporating system, non-condensable gas and cold liquid heat transfer in the heating chamber. The utility model discloses the non-condensable gas recovery system of vaporization system, this system application scope is wide, the load capacity that shocks resistance is strong, the running cost is low, easy operation, is applicable to the non-condensable gas of handling vaporization system production.
Description
Technical Field
The utility model relates to a heat source recovery recycles the technique, especially relates to an evaporation system noncondensable gas recovery system.
Background
In the evaporation process of equipment, a certain amount of high-temperature non-condensable gas is generated in the process of treating the landfill leachate by adopting a core process technology of MVR (mechanical vapor recompression) + VP (scrubbing). The main components of the non-condensable gas comprise most of water vapor, a small amount of distilled water and part of the non-condensable gas. The main treatment methods at present are the direct discharge method and the heat exchange method.
The direct discharge method is to directly discharge the non-condensable gas into the atmosphere by using the pressure difference between the system and the atmosphere; the first method is that the atmosphere causes pollution; secondly, the non-condensable gas can generate condensed water in the process of contacting with the atmosphere, a large amount of condensed water can be generated in the long-term operation, pollution can be caused, and heat loss can be caused.
The heat exchange method is to utilize cold water to exchange heat with the non-condensable gas, so as to reduce the temperature of the non-condensable gas; this solution has the disadvantage of requiring a source of cold water, cooling tower equipment, etc., which results in high costs and also in heat losses.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide an evaporating system noncondensable gas recovery system to the problem that present evaporating system noncondensable gas processing method easily caused atmospheric pollution and calorific loss, this system application scope is wide, the load capacity that shocks resistance is strong, the running cost is low, easy operation, is applicable to the noncondensable gas of handling evaporating system production.
In order to achieve the above object, the utility model adopts the following technical scheme: a non-condensable gas recovery system of an evaporation system comprises a first separation chamber, a first circulating pump, a first heating chamber, a first distilled water tank, a first distilled water pump, a first steam compressor, a second separation chamber, a second circulating pump, a second heating chamber, a second distilled water tank, a second distilled water pump and a second steam compressor;
the first separation chamber inlet is communicated with a raw steam pipeline, 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 inlet (steam inlet) of the hot side of the first heating chamber; the condensed water outlet of the first heating chamber is communicated with the inlet of a first distilled water tank, and the outlet of the first distilled water tank is communicated with the inlet of a first distilled water pump;
the inlet of the second separation chamber is communicated with a raw steam pipeline, the bottom circulating liquid outlet of the second separation chamber is communicated with the cold side inlet of the second heating chamber through a second circulating pump, and the hot 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 inlet (steam inlet) of the hot side of the second heating chamber; the condensed water outlet of the second heating chamber is communicated with the inlet of a second distilled water tank, and the outlet of the second distilled water tank is communicated with the inlet of a second distilled water pump;
and the non-condensable gas outlet (hot side outlet) of the first heating chamber is communicated with the non-condensable gas inlet (hot side inlet) of the second heating chamber.
Further, the evaporation device is communicated with the first separation chamber and the second separation chamber through a steam generation pipeline, namely a non-condensable gas source is generated in the main evaporation process.
Further, a wire mesh demister and a spraying assembly are arranged in the first separation chamber and the second separation chamber, wherein the wire mesh demister is arranged at the upper part of the separation chamber, and the spraying assembly is arranged at the upper part of the wire mesh demister.
Furthermore, the first heating chamber and the second heating chamber are both tube type heat exchangers.
Furthermore, heat exchange tubes, end sockets and baffle plates are arranged in the first heating chamber and the second heating chamber, wherein the heat exchange tubes are distributed in the heating chambers, the end sockets are arranged at two ends of the heating chambers, and the baffle plates are arranged in the middle of the end sockets at one end of the heating chambers.
A non-condensable gas recovery process of an evaporation system comprises the following steps: concentrated solution generated by the first separation chamber is conveyed to the first heating chamber through the first circulating pump, heated to an overheated state through high-temperature steam in the shell pass of the first heating chamber and returned to the first separation chamber, because the pressure in the first separation chamber is lower, the material in the overheated state is subjected to flash evaporation, and secondary steam generated by flash evaporation is returned to the shell pass of the first heating chamber through the first steam compressor and continuously exchanges heat with low-temperature material; condensed water after heat exchange of high-temperature steam in the shell side of the first heating chamber enters a first distilled water tank and is conveyed to a subsequent working section by a first distilled water pump;
concentrated solution generated by the second separation chamber is conveyed to the second heating chamber through the second circulating pump, heated to an overheated state through high-temperature steam in the shell pass of the second heating chamber and returned to the second separation chamber, and due to the fact that the pressure in the second separation chamber is low, materials in the overheated state are subjected to flash evaporation, secondary steam generated by flash evaporation returns to the shell pass of the second heating chamber through the second steam compressor, and heat exchange with low-temperature materials is continued; the non-condensable gas in the first heating chamber enters a non-condensable gas inlet of the second heating chamber to exchange heat with the low-temperature material; and the condensed water after the heat exchange of the high-temperature steam in the shell pass of the second heating chamber enters a second distilled water tank and is conveyed to a subsequent working section by a second distilled water pump.
And starting a circulating pump of the cooling equipment for circulation, then feeding the main body noncondensable gas generated by the running equipment into the heating chamber through a steam pipeline to heat the heating chamber, wherein the condensed water generated in the heating process overflows into the distilled water tank.
Further, the amount of non-condensable gas in the non-condensable gas is 0.015-0.020 times of the treatment amount of the evaporation equipment.
Further, the temperature of the non-condensable gas is 108-112 ℃.
Further, the non-condensable gas exchanges heat with the cold liquid in the heating chamber (second heating chamber).
The utility model discloses the non-condensable gas recovery system of vaporization system specifically is a non-condensable gas of vaporization system is used as the system of heat source, compares with prior art, has following advantage:
1) the utility model discloses a process and system that evaporating system noncondensable gas was used as the heat source utilize the high temperature noncondensable gas that the operation equipment produced to heat the heating chamber, need not to throw and add chemical agent, only a small amount of power consumption, and the running cost is low.
2) The utility model discloses a technology and system that evaporating system noncondensable gas was used as the heat source utilize shell and tube heat exchanger to retrieve the heat source, avoid calorific loss.
To sum up, the utility model discloses the non-condensable gas recovery system of vaporization system has energy saving, running cost is low, easy operation, technological process science, reasonable advantage.
Drawings
Fig. 1 is a schematic view of the non-condensable gas recovery system of the evaporation system of the present invention.
Wherein: 1. a first separation chamber; 2. a first circulation pump; 3. a first heating chamber; 4. a first distilled water tank; 5. a first distilled water pump; 6. a first vapor compressor; 7. a second separation chamber; 8. a second circulation pump; 9. A second heating chamber; 10. a second distilled water tank; 11. a second distilled water pump; 12. a second vapor compressor.
Detailed Description
The invention is further illustrated below with reference to the following examples:
example 1
The embodiment discloses a non-condensable gas recovery system of an evaporation system, which has a structure shown in fig. 1 and comprises a forced circulation system, wherein the forced circulation system comprises a first separation chamber 1, a first circulating pump 2, a first heating chamber 3, a first distilled water tank 4, a first distilled water pump 5, a first steam compressor 6, a second separation chamber 7, a second circulating pump 8, a second heating chamber 9, a second distilled water tank 10, a second distilled water pump 11 and a second steam compressor 12;
an inlet of the first separation chamber 1 is communicated with a raw steam pipeline, a bottom circulating liquid outlet of the first separation chamber 1 is communicated with a cold side inlet of the first heating chamber 3 through a first circulating pump 2, and a cold side outlet of the first heating chamber 3 is communicated with a 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 6, and the outlet of the first steam compressor 6 is communicated with the inlet (steam inlet) of the hot side of the first heating chamber 3; a condensed water outlet of the first heating chamber 3 is communicated with an inlet of a first distilled water tank 4, and an outlet of the first distilled water tank 4 is communicated with an inlet of a first distilled water pump 5;
an inlet of the second separation chamber 7 is communicated with a raw steam pipeline, a circulating liquid outlet at the bottom of the second separation chamber 7 is communicated with a cold side inlet of a second heating chamber 9 through a second circulating pump 8, and a hot side outlet of the second heating chamber 9 is communicated with a circulating liquid inlet of the second separation chamber 7; the steam outlet of the second separation chamber 7 is communicated with the inlet of a second steam compressor 12, and the outlet of the second steam compressor 12 is communicated with the hot side inlet (steam inlet) of the second heating chamber 9; a condensed water outlet of the second heating chamber 9 is communicated with an inlet of a second distilled water tank 10, and an outlet of the second distilled water tank 10 is communicated with an inlet of a second distilled water pump 11;
the non-condensable gas outlet (hot side outlet) of the first heating chamber 3 is communicated with the non-condensable gas inlet (hot side inlet) of the second heating chamber 9.
The evaporation device is communicated with the first separation chamber 1 and the second separation chamber 7 through a steam generation pipeline, namely, a non-condensable gas source is generated in the main evaporation process.
And a wire mesh demister and a spraying assembly are arranged in the first separation chamber 1 and the second separation chamber 7. The first heating chamber 3 and the second heating chamber 9 are both tube type heat exchangers. And heat exchange tubes, end sockets and baffle plates are arranged in the first heating chamber 3 and the second heating chamber 9.
The non-condensable gas recovery process of the evaporation system comprises the following steps of: the raw steam enters the first separation chamber 1 to heat the system, concentrated liquid generated by the first separation chamber 1 is conveyed to the first heating chamber 3 through the first circulating pump 2, the concentrated liquid is heated to an overheated state through high-temperature steam in the shell pass of the first heating chamber 3 and then returns to the first separation chamber 1 through the circulating liquid inlet of the first separation chamber 1, the material in the overheated state is subjected to flash evaporation due to the fact that the pressure in the first separation chamber 1 is small, and secondary steam generated by the flash evaporation returns to the shell pass of the first heating chamber 3 through the steam outlet of the first separation chamber 1, the first steam compressor 6 and the steam inlet of the first heating chamber 3 to continuously exchange heat with the low-temperature material. Condensed water after heat exchange of high-temperature steam in the shell pass of the first heating chamber 3 enters a first distilled water tank 4 and is conveyed to a subsequent working section by a first distilled water pump 5.
Raw steam enters a second separation chamber 7 to heat the system, concentrated liquid generated by the second separation chamber 7 is conveyed to a second heating chamber 9 through a second circulating pump 8, the concentrated liquid is heated to an overheated state through high-temperature steam in the shell pass of the second heating chamber 9 and then returns to the second separation chamber 7 through a circulating liquid inlet of the second separation chamber 7, as the pressure in the second separation chamber 7 is lower, the material in the overheated state is subjected to flash evaporation, and secondary steam generated by flash evaporation returns to the shell pass of the second heating chamber 9 through a steam outlet of the second separation chamber 7, a second steam compressor 12 and a steam inlet of the second heating chamber 9 to continuously exchange heat with low-temperature material; the non-condensable gas in the first heating chamber 3 enters a non-condensable gas inlet of the second heating chamber 9 to exchange heat with the low-temperature material; the condensed water after the heat exchange of the high-temperature steam in the shell pass of the second heating chamber 9 enters a second distilled water tank 10 and is conveyed to a subsequent working section by a second distilled water pump 11.
And starting a circulating pump of the cooling equipment for circulation, then feeding the main body noncondensable gas generated by the running equipment into the heating chamber through a steam pipeline to heat the heating chamber, wherein the condensed water generated in the heating process overflows into the distilled water tank.
The amount of non-condensable gas in the non-condensable gas is 0.015-0.020 times of that of evaporation equipment. The temperature of the non-condensable gas is 108-112 ℃. The non-condensable gas exchanges heat with the cold liquid in the heating chamber (the second heating chamber 9).
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 (5)
1. The non-condensable gas recovery system of the evaporation system is characterized by comprising a first separation chamber (1), a first circulating pump (2), a first heating chamber (3), a first distilled water tank (4), a first distilled water pump (5), a first steam compressor (6), a second separation chamber (7), a second circulating pump (8), a second heating chamber (9), a second distilled water tank (10), a second distilled water pump (11) and a second steam compressor (12);
the inlet of the first separation chamber (1) is communicated with a raw steam pipeline, the bottom circulating liquid outlet of the first separation chamber (1) is communicated with the cold side inlet of the first heating chamber (3) through a first circulating pump (2), and the cold side outlet of the first heating chamber (3) 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 (6), and the outlet of the first steam compressor (6) is communicated with the hot side inlet of the first heating chamber (3); a condensed water outlet of the first heating chamber (3) is communicated with an inlet of a first distilled water tank (4), and an outlet of the first distilled water tank (4) is communicated with an inlet of a first distilled water pump (5);
an inlet of the second separation chamber (7) is communicated with a raw steam pipeline, a circulating liquid outlet at the bottom of the second separation chamber (7) is communicated with a cold side inlet of a second heating chamber (9) through a second circulating pump (8), and a hot side outlet of the second heating chamber (9) is communicated with a circulating liquid inlet of the second separation chamber (7); the steam outlet of the second separation chamber (7) is communicated with the inlet of a second steam compressor (12), and the outlet of the second steam compressor (12) is communicated with the hot side inlet of a second heating chamber (9); the condensed water outlet of the second heating chamber (9) is communicated with the inlet of a second distilled water tank (10), and the outlet of the second distilled water tank (10) is communicated with the inlet of a second distilled water pump (11);
the non-condensable gas outlet of the first heating chamber (3) is communicated with the non-condensable gas inlet of the second heating chamber (9).
2. The non-condensable gas recovery system of the evaporation system as claimed in claim 1 wherein the evaporation device is in communication with the first separation chamber (1) and the second separation chamber (7) through a steam generating line.
3. The non-condensable gas recovery system of the evaporation system as claimed in claim 1, wherein a wire mesh demister and a spray assembly are arranged in the first separation chamber (1) and the second separation chamber (7).
4. The non-condensable gas recovery system of the evaporation system as claimed in claim 1 wherein the first heating chamber (3) and the second heating chamber (9) are both tube type heat exchangers.
5. The non-condensable gas recovery system of the evaporation system as claimed in claim 1, wherein heat exchange tubes, end sockets and baffles are arranged in the first heating chamber (3) and the second heating chamber (9).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023082089.0U CN214512794U (en) | 2020-12-21 | 2020-12-21 | Non-condensable gas recovery system of evaporation system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202023082089.0U CN214512794U (en) | 2020-12-21 | 2020-12-21 | Non-condensable gas recovery system of evaporation system |
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| CN214512794U true CN214512794U (en) | 2021-10-29 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112619196A (en) * | 2020-12-21 | 2021-04-09 | 大连广泰源环保科技有限公司 | Non-condensable gas recovery process and system for evaporation system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112619196A (en) * | 2020-12-21 | 2021-04-09 | 大连广泰源环保科技有限公司 | Non-condensable gas recovery process and system for evaporation system |
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