CN212327892U - Energy-saving flue gas carbon dioxide recovery system - Google Patents
Energy-saving flue gas carbon dioxide recovery system Download PDFInfo
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- CN212327892U CN212327892U CN202020888308.5U CN202020888308U CN212327892U CN 212327892 U CN212327892 U CN 212327892U CN 202020888308 U CN202020888308 U CN 202020888308U CN 212327892 U CN212327892 U CN 212327892U
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Abstract
The utility model belongs to the technical field of chemical gas recovery, in particular to an energy-saving flue gas carbon dioxide recovery system, which comprises a flue gas regenerator, a gas-liquid separator, a washing absorption tower and a regeneration tower; a washing section, an absorption section and a cooling section are sequentially arranged in the washing absorption tower from top to bottom; the flue gas regenerator is communicated with the cooling section; the absorption section is communicated with the upper part of the gas-liquid separator through a flue gas regenerator; the bottom of the gas-liquid separator is communicated with the regeneration tower; the regeneration tower is communicated with the absorption section. The utility model discloses to cool off, washing, absorb and collect in a tower, process flow is simple, reduces the technological resistance, and gas conveying equipment is few, and consumption of power reduces, and adopts hierarchical regeneration, practices thrift regeneration heat and flue gas cooling capacity, and regeneration is thorough, realizes energy-conserving purpose.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry gas recovery, especially, relate to an energy-saving flue gas carbon dioxide recovery system.
Background
The smoke is a mixture of gas and smoke dust and is a main reason for polluting the atmosphere of a residential area, the smoke contains a large amount of CO2, and if the content of CO2 in the air is as high as 7-10%, people can lose consciousness within a few minutes and die; if the flue gas is directly discharged into the atmosphere, a large amount of toxic CO2 can cause harm to human bodies, and simultaneously, the waste of resources can be caused; therefore, the carbon dioxide in the flue gas needs to be recycled, and the common decarburization methods include a chemical absorption method, a physical separation method and a membrane treatment method, but in the actual treatment, the carbon dioxide in the flue gas is often recycled by the chemical absorption method due to the strong selectivity of the chemical absorption reaction, high product purity, mature process, simple equipment and high recovery rate.
When the chemical adsorption method is used for recovering carbon dioxide in flue gas, an absorption tower, a regeneration tower, a cooling tower, a washing tower and the like are needed, and washing, absorption, cooling and regeneration are completed in independent equipment in the absorption process, so that the existing recovery system has the defects of long process flow, large resistance, more conveying equipment and large power consumption, and meanwhile, the existing recovery system is not thorough in regeneration and large in heat and cold consumption.
SUMMERY OF THE UTILITY MODEL
In the carbon dioxide recovery in to current flue gas, technological process is long, equipment is many, power and energy consumption are big to and the incomplete technical problem of regeneration, the utility model provides an energy-saving flue gas carbon dioxide recovery system will cool off, wash, absorb and collect in a tower, and technological process is simple, reduces the technological resistance, and gas conveying equipment is few, and consumption of power reduces, and adopts hierarchical regeneration, practices thrift regeneration heat and flue gas cooling capacity, and regeneration is thorough.
In order to realize the purpose, the utility model discloses a technical scheme is:
an energy-saving flue gas carbon dioxide recovery system comprises a flue gas regenerator, a gas-liquid separator, a washing absorption tower and a regeneration tower; a washing section, an absorption section and a cooling section are sequentially arranged in the washing absorption tower from top to bottom; the flue gas regenerator is communicated with the cooling section; the absorption section is communicated with the upper part of the gas-liquid separator through a flue gas regenerator; the bottom of the gas-liquid separator is communicated with the regeneration tower; the regeneration tower is communicated with the absorption section.
Further, the energy-saving flue gas carbon dioxide recovery system also comprises a lean solution cooler and a lean and rich solution heat exchanger; the bottom of the gas-liquid separator is communicated with the regeneration tower through a lean-rich liquid heat exchanger; the regeneration tower is communicated with the absorption section through a lean-rich liquid heat exchanger and a lean liquid cooler in sequence.
Further, the energy-saving flue gas carbon dioxide recovery system also comprises a carbon dioxide cooler and a separator; the carbon dioxide cooler is respectively communicated with the top of the gas-liquid separator, the top of the regeneration tower and the side part of the separator; the bottom of the separator is communicated with the regeneration tower.
Further, the energy-saving flue gas carbon dioxide recovery system also comprises a reboiler communicated with the regeneration tower.
Furthermore, the energy-saving flue gas carbon dioxide recovery system also comprises a washing water heat exchanger and a washing water pump which are respectively communicated with the washing section; and the washing water pump is communicated with the washing water heat exchanger.
Furthermore, the energy-saving flue gas carbon dioxide recovery system also comprises a cooling water heat exchanger and a cooling water pump which are respectively communicated with the cooling section; and the cooling water pump is communicated with the cooling water heat exchanger.
Furthermore, the energy-saving flue gas carbon dioxide recovery system also comprises an exhaust pipeline arranged at the bottom of the flue gas regenerator.
The utility model has the advantages that:
1. in the utility model, a washing section, an absorption section and a cooling section are arranged in the washing absorption tower from top to bottom in sequence; the functions of washing, absorption and cooling are realized simultaneously by washing one device of the absorption tower, the two towers are integrated, the process resistance is reduced, the consumption of gas conveying equipment and power equipment is reduced, and the recovery process is simplified.
2. In the utility model, the flue gas regenerator is communicated with the cooling section; the absorption section is communicated with the top of the gas-liquid separator through a flue gas regenerator; recovering heat in the flue gas for primary regeneration of absorption liquid in a flue gas regenerator; the heat of the flue gas is transferred to primary regeneration, the heat is recycled, the consumption of cooling capacity of the flue gas is saved, and the energy consumption of a system is reduced.
3. In the utility model, the top of the gas-liquid separator is communicated with the regeneration tower; the regeneration tower is communicated with the absorption section. The primary regenerated liquid after passing through the flue gas regenerator enters a regeneration tower for secondary regeneration, and meanwhile, the primary regenerated liquid and the secondary regenerated liquid entering the absorption section perform heat exchange to transfer the heat of the secondary regenerated liquid to the primary in-situ regenerated liquid; the heat is recycled, the cold quantity required by cooling the secondary regenerated liquid is reduced, and the energy consumption of the system is reduced.
4. In the utility model, the flue gas regenerator and the regeneration tower form two-stage regeneration; in each stage of regeneration process, the heat is recycled, the consumption of the heat and the cold is reduced, the absorption liquid is regenerated more thoroughly through the stage regeneration, the heat of the system is fully utilized, the heat and the cold are saved, and the purpose of saving energy is achieved.
Drawings
FIG. 1 is a schematic view of a system for recovering sulfur dioxide from flue gas;
wherein:
1-flue gas regenerator; 2-gas-liquid separator; 3, a fan; 4-a liquid-rich pump; 5-washing the absorption tower; 6-washing water heat exchanger; 7-washing water pump; 8-lean liquor cooler; 9-cooling water heat exchanger; 10-cooling water pump; 11-lean-rich liquor heat exchanger; 12-barren liquor pump; 13-a regeneration column; 14-a carbon dioxide cooler; 15-a separator; 16-a vacuum pump; 17-a reboiler; 18-a liquid storage tank; 19-liquid storage pump.
Detailed Description
The present invention will now be described in detail with reference to the accompanying drawings and specific embodiments.
The utility model provides an energy-saving flue gas carbon dioxide recovery system, which comprises a flue gas regenerator 1, a gas-liquid separator 2, a washing absorption tower 5 and a regeneration tower 13; a washing section, an absorption section and a cooling section are sequentially arranged in the washing absorption tower 5 from top to bottom; the flue gas regenerator 1 is communicated with the cooling section; the absorption section is communicated with a gas-liquid separator 2 through a flue gas regenerator 1; the top of the gas-liquid separator 2 is communicated with a regeneration tower 13; the regenerator column 13 is in communication with the absorption section.
The energy-saving flue gas carbon dioxide recovery system provided by the utility model also comprises a barren solution cooler 8 and a barren and rich solution heat exchanger 11; the bottom of the gas-liquid separator 2 is communicated with a regeneration tower 13 through a lean-rich liquid heat exchanger 11; the regeneration tower 13 is communicated with the absorption section through a lean-rich liquid heat exchanger 11 and a lean liquid cooler 8 in sequence.
The energy-saving flue gas carbon dioxide recovery system provided by the utility model also comprises a carbon dioxide cooler 14 and a separator 15; the carbon dioxide cooler 14 is respectively communicated with the top of the gas-liquid separator 2, the top of the regeneration tower 13 and the side of the separator 15; the bottom of the separator 15 communicates with the regeneration column 13.
The utility model provides an energy-saving flue gas carbon dioxide recovery system still includes the reboiler 17 that is linked together with regenerator 13.
The energy-saving flue gas carbon dioxide recovery system provided by the utility model also comprises a washing water heat exchanger 6 and a washing water pump 7 which are respectively communicated with the washing section; and the washing water pump 7 is communicated with the washing water heat exchanger 6.
The energy-saving flue gas carbon dioxide recovery system provided by the utility model also comprises a cooling water heat exchanger 9 and a cooling water pump 10 which are respectively communicated with the cooling section; and the cooling water pump 10 is communicated with the cooling water heat exchanger 9.
The utility model provides an energy-saving flue gas carbon dioxide recovery system is still including setting up the pipeline of taking out to the greatest extent in 1 bottom of flue gas regenerator.
The utility model provides an energy-saving flue gas carbon dioxide recovery process, including following step:
1) the flue gas enters a cooling section of a washing absorption tower 5 after being subjected to heat exchange and temperature reduction by a flue gas regenerator 1; the cooled cooling flue gas passes through an absorption section of the washing absorption tower 5, and carbon dioxide gas in the cooling flue gas is absorbed by the absorbent under the action of the absorbent to obtain absorption pregnant solution; the cooling flue gas which is not absorbed by the absorbent is discharged out of the washing absorption tower 5 after being washed by the washing section of the washing absorption tower 5;
2) the absorption rich solution is sent to a flue gas regenerator 1 for primary regeneration to obtain primary regenerated solution and primary carbon dioxide regenerated gas; the primary regenerated liquid is sent to a regeneration tower 13 for secondary regeneration after heat exchange and temperature rise to obtain secondary regenerated liquid and secondary carbon dioxide regenerated gas;
3) the secondary regenerated liquid and the primary regenerated liquid are subjected to heat exchange and temperature reduction and then are sent to an absorption section of a washing absorption tower 5 to be used as an absorbent; the primary carbon dioxide regenerated gas and the secondary carbon dioxide regenerated gas are both cooled by a carbon dioxide cooler 14 to generate carbon dioxide gas and condensate, and the carbon dioxide gas is discharged by vacuum compression; the condensate is sent to the regeneration tower 13.
The utility model provides an in step 1), the washing section and the cooling zone of washing absorption tower 5 all adopt the desalinized water cooling circulation washing.
The utility model provides an in step 2), in the secondary regeneration process, heat the tower cauldron of regenerator 13 through letting in steam or transformation gas in to reboiler 17.
Example 1
Referring to fig. 1, the energy-saving flue gas carbon dioxide recovery system provided by the present embodiment includes a flue gas regenerator 1, a gas-liquid separator 2, a scrubbing-absorbing tower 5, a regeneration tower 13, a lean liquid cooler 8, a lean rich liquid heat exchanger 11, a carbon dioxide cooler 14, a separator 15, and a reboiler 17.
In this embodiment, the washing absorption tower 5 is provided with a washing section, an absorption section and a cooling section from top to bottom in sequence.
In the embodiment, the flue gas regenerator 1 is communicated with the cooling section through a fan 3; the bottom of the gas-liquid separator 2 is communicated with the upper part of a regeneration tower 13 after passing through a rich solution pump 4 and a lean and rich solution heat exchanger 11; the top of the gas-liquid separator 2 is communicated with a carbon dioxide cooler 14; the lower part of the absorption section is communicated with the upper part of the gas-liquid separator 2 through the flue gas regenerator 1.
In the embodiment, outside the washing section of the washing absorption tower 5, a washing water heat exchanger 6 is communicated with the upper part of a tower plate of the washing section; the washing water pump 7 is communicated with the lower part of the tower plate of the washing section; and the washing water heat exchanger 6 and the washing water pump 7 are communicated. Outside the cooling section of the washing absorption tower 5, a cooling water heat exchanger 9 is communicated with the upper tower side of the cooling section; the cooling water pump 10 is communicated with the lower tower side of the cooling section, and the cooling water pump 10 is communicated with the cooling water heat exchanger 9.
In this embodiment, the lower part of the regeneration tower 13 is communicated with the upper part of the absorption section through the lean solution pump 12, the lean and rich solution heat exchanger 11 and the lean solution cooler 8, and the top of the regeneration tower 13 is communicated with the carbon dioxide cooler 14; the tower bottom of the regeneration tower 13 returns to the upper tower plate of the tower bottom of the regeneration tower 13 after passing through a reboiler 17.
In the present embodiment, the carbon dioxide cooler 14 communicates with the side of the separator 15; the bottom of the separator 15 is communicated with the upper part of the regeneration tower 13; the top of the separator 15 is in communication with a vacuum pump 16.
Example 2
On the basis of embodiment 1, in this embodiment, the energy-saving flue gas carbon dioxide recovery system further includes an exhaust line disposed at the bottom of the flue gas regenerator 1.
In this embodiment, the upper portion of the gas-liquid separator 2 is further provided with a desalted water pipeline communicated with the gas-liquid separator 2, and desalted water is filled when the carbon dioxide production device is stopped, so that the flue gas regenerator 1 does not burn dry and the equipment is protected.
When the method is implemented, the solution is completely pumped out when the carbon dioxide production device is stopped, and desalted water is filled into the gas-liquid separator 2 to protect equipment. The carbon dioxide production device stops completely pumping the solution, and simultaneously desalted water is added to generate steam, so that the equipment is prevented from being damaged by dry burning of the flue gas regenerator 1, and the steam is discharged from the top of the gas-liquid separator 2.
In this embodiment, the energy-saving flue gas carbon dioxide recovery system further includes a liquid storage tank 18 and a liquid storage pump 19; the bottom of the flue gas regenerator 1 is connected with a liquid storage pump 19 and a liquid storage tank 18 in sequence, the liquid storage pump 19 is connected with the lean-rich liquid heat exchanger 11, and a valve is arranged on a connecting pipeline and used for liquid supplement.
Specifically, the solution pumped from the pumping line at the bottom of the flue gas regeneration gas 1 passes through a liquid storage pump 19, or directly enters the liquid storage tank 18 from the upper part of the liquid storage tank 18 for storage; or the mixture enters a regeneration tower 13 through a lean-rich solution heat exchanger 11 for regeneration and liquid supplementation; in particular, the adjustment can be carried out according to the actual condition of the process.
Example 3
By way of specific example, a specific recovery process of the energy-saving flue gas carbon dioxide recovery system provided in embodiment 1 and embodiment 2 is described.
In this example, the conversion flue gas (containing nitrogen N) from the carbon dioxide production process2Carbon dioxide CO2And a small amount of oxygen O2) The temperature is about 120 ℃ and 160 ℃, and the pressure is 0.8-1.2 kPa; at present, carbon dioxide in the waste gas needs to be recovered, and the specific recovery flow is as follows:
the flue gas passes through the flue gas regenerator 1, and then is taken away by the flue gas regenerator 1 to obtain regenerated flue gas, the regenerated flue gas is sent to a cooling section at the lower part of the washing absorption tower 5 through the fan 3, outside the cooling section, washing water enters the inside of the cooling section after being cooled by the cooling water pump 10 and the cooling water heat exchanger 9 to cool the regenerated flue gas, the washing water takes out heat in the cooled regenerated flue gas, and the cooled regenerated flue gas is cooled by the cooling water pump 10 and the cooling water heat exchanger 9 and then enters the cooling section again, and the heat in the regenerated flue gas is taken out through the circulating cooling of the washing water; the cooled cooling flue gas flows to an absorption section in the middle of the washing absorption tower 5 from the cooling section;
reacting with absorbent (compound amine solution) in the absorption section, and cooling carbon dioxide CO in the cooled flue gas2Absorbed by absorbent to obtain CO rich2The absorption rich liquid of (1); the unabsorbed cooling flue gas is discarded and continuously enters a washing section at the upper part of the washing absorption tower 5; outside the washing section, the washing water enters the washing section to wash unabsorbed cooling flue gas after being cooled by a washing water pump 7 and a washing water heat exchanger 6, and the unabsorbed cooling flue gas is cooled by the washing waterThe absorption rich liquid carried by the raw flue gas is washed, and the unabsorbed cooling flue gas (mainly nitrogen N)2And a small amount of oxygen O2) The waste gas is discharged from the top of the washing absorption tower 5, and the washing water enters the washing section again after passing through a washing water pump 7 and a washing water heat exchanger 6, so that the circular washing is realized;
the absorption rich solution passes through a flue gas regenerator 1 to exchange heat with flue gas entering the flue gas regenerator 1 and raise the temperature, and meanwhile, the absorption rich solution is regenerated in the flue gas regenerator 1 for the first time and passes through a gas-liquid separator 2 to obtain a primary regenerated solution (containing part of carbon dioxide and an absorbent) and primary regenerated gas (containing part of carbon dioxide and the absorbent); the primary regeneration gas is discharged from the top of the gas-liquid separator 2, cooled by a carbon dioxide cooler 14 and then enters a separator 15 for separation, and the condensate enters the upper part of the regeneration tower 13 from the bottom of the separator 15 for continuous regeneration; the carbon dioxide gas is recovered from the top of the separator 15 after the negative pressure is reduced by a vacuum pump 16; the vacuum reduction of the negative pressure is beneficial to the regeneration of the carbon dioxide in the regeneration tower 13;
the primary regeneration liquid sequentially passes through a rich liquid pump 4 and a lean rich liquid heat exchanger 11 from the bottom of the gas-liquid separator 2 and then enters the upper part of a regeneration tower 13 for secondary regeneration to obtain secondary regeneration liquid (containing a very small amount of carbon dioxide and a large amount of absorbent, namely absorption lean liquid) and secondary regeneration gas (containing a large amount of carbon dioxide and a small part of absorbent); the secondary regenerated liquid contains a small amount of carbon dioxide and a large amount of absorbent, so that the secondary regenerated liquid can be used as the absorbent, and therefore, the secondary regenerated liquid enters the upper part of the absorption section from the lower part of the regeneration tower 13 after passing through the lean liquid pump 12, the lean rich liquid heat exchanger 11 and the lean liquid cooler 8, the carbon dioxide in the cooled regenerated flue gas is absorbed, and the absorbent is regenerated and recycled; secondary regeneration gas (carbon dioxide and a small part of absorption liquid) is discharged from the top of the regeneration tower 13, is cooled by a carbon dioxide cooler 14 and then enters a separator 15 for separation, and condensate enters the upper part of the regeneration tower 13 from the bottom of the separator 15 for continuous regeneration; the carbon dioxide gas is recovered from the top of the separator 15 after the negative pressure is reduced by a vacuum pump 16; the reduction of the negative pressure by the vacuum is favorable for the regeneration of the carbon dioxide in the regeneration tower 13.
In this embodiment, the bottom of the regeneration tower 13 is heated by the reboiler 17, and the liquid from the bottom of the regeneration tower 13 and the steam or reformed gas introduced into the reboiler 17 are heated by heat exchange; and then returned to the regeneration tower 13. The secondary regeneration gas of the regeneration tower 13 is cooled by being combined with the primary regeneration gas from the flue gas regenerator, and is sent to a compressor through a vacuum fan.
In the embodiment, in the absorption and regeneration treatment process of the absorption liquid, when the temperature of the absorption liquid is 20-40 ℃ and normal temperature, a forward reaction occurs, and carbon dioxide is chemically absorbed by an absorbent (a composite amine solution); and heating the absorption rich liquid after absorbing the carbon dioxide to perform a reverse reaction, desorbing the absorption rich liquid to obtain the product carbon dioxide, and simultaneously regenerating the absorbent.
In this embodiment, the bottom of the flue gas regenerator 1 is provided with a drain line, when the carbon dioxide device is stopped, the solution in the flue gas regenerator 1 is drained, and desalted water is filled to protect the equipment and avoid dry burning.
In the embodiment, a flue gas regenerator 1 is connected with the bottom of an absorption section, and an absorbent (absorption rich liquid) for absorbing flue gas is subjected to two-stage regeneration by the flue gas regenerator and a regeneration tower in sequence to obtain a secondary regeneration liquid (namely absorption barren liquid) which is sent to the upper part of the absorption section after being cooled; vacuumizing carbon dioxide gas in the primary regeneration gas and the secondary regeneration gas by using a vacuum pump to accelerate regeneration, and sending the carbon dioxide gas to a post-process after the carbon dioxide gas passes through the vacuum pump;
the utility model provides an energy-saving flue gas carbon dioxide recovery system and a recovery process, which has the principle that the carbon dioxide in the cooled flue gas is absorbed by a compound amine solution, and the unabsorbed gas in the flue gas is discharged from the top of a washing absorption tower; the absorbent absorbing carbon dioxide is subjected to two-stage heating regeneration to release the absorbed carbon dioxide, and the solution after release can be stored and used as circulating washing water. The utility model integrates cooling, washing and cooling in one tower, reduces the process resistance, reduces the gas conveying machinery and the power consumption, and simplifies the flow; and the graded regeneration is adopted, so that the heat and the cooling capacity are saved, and the two-stage regeneration is adopted, so that the absorbent is regenerated thoroughly.
Claims (7)
1. The utility model provides an energy-saving flue gas carbon dioxide recovery system which characterized in that: the energy-saving flue gas carbon dioxide recovery system comprises a flue gas regenerator (1), a gas-liquid separator (2), a washing absorption tower (5) and a regeneration tower (13);
a washing section, an absorption section and a cooling section are sequentially arranged in the washing absorption tower (5) from top to bottom;
the flue gas regenerator (1) is communicated with the cooling section; the absorption section is communicated with the upper part of the gas-liquid separator (2) through a flue gas regenerator (1); the bottom of the gas-liquid separator (2) is communicated with a regeneration tower (13); the regeneration tower (13) is communicated with the absorption section.
2. The energy-saving flue gas carbon dioxide recovery system of claim 1, characterized in that: the energy-saving flue gas carbon dioxide recovery system also comprises a lean solution cooler (8) and a lean and rich solution heat exchanger (11); the bottom of the gas-liquid separator (2) is communicated with a regeneration tower (13) through a lean-rich liquid heat exchanger (11); the regeneration tower (13) is communicated with the absorption section through a lean-rich liquid heat exchanger (11) and a lean liquid cooler (8) in sequence.
3. The energy-saving flue gas carbon dioxide recovery system of claim 2, characterized in that: the energy-saving flue gas carbon dioxide recovery system also comprises a carbon dioxide cooler (14) and a separator (15); the carbon dioxide cooler (14) is respectively communicated with the top of the gas-liquid separator (2), the top of the regeneration tower (13) and the side of the separator (15); the bottom of the separator (15) is communicated with the regeneration tower (13).
4. The energy-saving flue gas carbon dioxide recovery system of claim 3, characterized in that: the energy-saving flue gas carbon dioxide recovery system also comprises a reboiler (17) communicated with the regeneration tower (13).
5. The energy-saving flue gas carbon dioxide recovery system of claim 4, characterized in that: the energy-saving flue gas carbon dioxide recovery system also comprises a washing water heat exchanger (6) and a washing water pump (7) which are respectively communicated with the washing section; and the washing water pump (7) is communicated with the washing water heat exchanger (6).
6. The energy-saving flue gas carbon dioxide recovery system of claim 5, characterized in that: the energy-saving flue gas carbon dioxide recovery system also comprises a cooling water heat exchanger (9) and a cooling water pump (10) which are respectively communicated with the cooling section; and the cooling water pump (10) is communicated with the cooling water heat exchanger (9).
7. The energy-saving flue gas carbon dioxide recovery system of claim 6, characterized in that: the energy-saving flue gas carbon dioxide recovery system also comprises an exhaust pipeline arranged at the bottom of the flue gas regenerator (1).
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| CN202020888308.5U CN212327892U (en) | 2020-05-22 | 2020-05-22 | Energy-saving flue gas carbon dioxide recovery system |
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| CN202020888308.5U CN212327892U (en) | 2020-05-22 | 2020-05-22 | Energy-saving flue gas carbon dioxide recovery system |
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