CN112619196A - Non-condensable gas recovery process and system for evaporation system - Google Patents
Non-condensable gas recovery process and system for evaporation system Download PDFInfo
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- CN112619196A CN112619196A CN202011513559.6A CN202011513559A CN112619196A CN 112619196 A CN112619196 A CN 112619196A CN 202011513559 A CN202011513559 A CN 202011513559A CN 112619196 A CN112619196 A CN 112619196A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
Abstract
The invention provides a non-condensable gas recovery process and a non-condensable gas recovery system of an evaporation system. The invention also discloses a non-condensable gas recovery process of the evaporation system, wherein the non-condensable gas exchanges heat with cold liquid in the heating chamber. The non-condensable gas recovery system of the evaporation system has the advantages of wide application range, strong impact load resistance, low operation cost and simple operation, and is suitable for treating the non-condensable gas generated by the evaporation system.
Description
Technical Field
The invention relates to a heat source recycling technology, in particular to a non-condensable gas recycling process and system for an evaporation 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.
Disclosure of Invention
The invention aims to provide a non-condensable gas recovery system of an evaporation system, which has the advantages of wide application range, strong impact load resistance, low operation cost and simplicity in operation and is suitable for treating non-condensable gas generated by the evaporation system, and aims to solve the problems that the existing non-condensable gas treatment method of the evaporation system is easy to cause air pollution and heat loss.
In order to achieve the purpose, the invention adopts the technical scheme that: 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 11;
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.
The invention also discloses a non-condensable gas recovery process of the evaporation system, which 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 9).
The invention relates to a process and a system for recovering noncondensable gas of an evaporation system, in particular to a process and a system for using the noncondensable gas of the evaporation system as a heat source,
1) the process and the system for using the non-condensable gas of the evaporation system as the heat source utilize the high-temperature non-condensable gas generated by the operating equipment to heat the heating chamber, do not need to add chemical agents, only have small power consumption and have low operating cost.
2) The technology and the system for using the non-condensable gas of the evaporation system as the heat source utilize the tube type heat exchanger to recover the heat source, thereby avoiding heat loss.
In conclusion, the non-condensable gas recovery process and the non-condensable gas recovery system of the evaporation system have the advantages of energy conservation, low operation cost, simplicity in operation and scientific and reasonable process flow.
Drawings
FIG. 1 is a schematic view of a 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 by the following examples:
example 1
The embodiment discloses a non-condensable gas recovery process and a non-condensable gas recovery system of an evaporation system, which have the structure shown in figure 1 and comprise 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; while the invention has been described in detail and with reference to the foregoing embodiments, it will 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; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (6)
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 system for recycling non-condensable gases in an evaporation system according to claim 1, wherein the evaporation device is in communication with the first separation chamber (1) and the second separation chamber (7) through a steam generation 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).
6. The non-condensable gas recovery process of the evaporation system is characterized by comprising the following steps of: 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011513559.6A CN112619196A (en) | 2020-12-21 | 2020-12-21 | Non-condensable gas recovery process and system for evaporation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011513559.6A CN112619196A (en) | 2020-12-21 | 2020-12-21 | Non-condensable gas recovery process and system for evaporation system |
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| CN112619196A true CN112619196A (en) | 2021-04-09 |
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| CN202011513559.6A Pending CN112619196A (en) | 2020-12-21 | 2020-12-21 | Non-condensable gas recovery process and system for evaporation system |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04140599A (en) * | 1990-09-28 | 1992-05-14 | Tokyo Gas Co Ltd | Decompression boiler type carburetor |
| JPH06159867A (en) * | 1992-11-30 | 1994-06-07 | Sanyo Electric Co Ltd | Absorption type refrigerating machine |
| US20040026225A1 (en) * | 2000-06-13 | 2004-02-12 | Jean-Paul Domen | Distillation method and appliances for fresh water production |
| CN109568997A (en) * | 2019-01-11 | 2019-04-05 | 江苏普格机械有限公司 | Seed precipitation solution seven imitates evaporating and concentrating process and seven effect tube-type down-flow evaporator groups |
| CN210385329U (en) * | 2019-06-25 | 2020-04-24 | 安徽同心新材料科技有限公司 | Noncondensable gas recovery unit of C5 petroleum resin flash distillation system |
| CN111115735A (en) * | 2020-02-26 | 2020-05-08 | 大连广泰源环保科技有限公司 | Two-stage forced circulation evaporation system and process for landfill leachate |
| CN214512794U (en) * | 2020-12-21 | 2021-10-29 | 大连广泰源环保科技有限公司 | Non-condensable gas recovery system of evaporation system |
-
2020
- 2020-12-21 CN CN202011513559.6A patent/CN112619196A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04140599A (en) * | 1990-09-28 | 1992-05-14 | Tokyo Gas Co Ltd | Decompression boiler type carburetor |
| JPH06159867A (en) * | 1992-11-30 | 1994-06-07 | Sanyo Electric Co Ltd | Absorption type refrigerating machine |
| US20040026225A1 (en) * | 2000-06-13 | 2004-02-12 | Jean-Paul Domen | Distillation method and appliances for fresh water production |
| CN109568997A (en) * | 2019-01-11 | 2019-04-05 | 江苏普格机械有限公司 | Seed precipitation solution seven imitates evaporating and concentrating process and seven effect tube-type down-flow evaporator groups |
| CN210385329U (en) * | 2019-06-25 | 2020-04-24 | 安徽同心新材料科技有限公司 | Noncondensable gas recovery unit of C5 petroleum resin flash distillation system |
| CN111115735A (en) * | 2020-02-26 | 2020-05-08 | 大连广泰源环保科技有限公司 | Two-stage forced circulation evaporation system and process for landfill leachate |
| CN214512794U (en) * | 2020-12-21 | 2021-10-29 | 大连广泰源环保科技有限公司 | Non-condensable gas recovery system of evaporation system |
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