CN111717915A - Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field - Google Patents
Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field Download PDFInfo
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- CN111717915A CN111717915A CN201910207460.4A CN201910207460A CN111717915A CN 111717915 A CN111717915 A CN 111717915A CN 201910207460 A CN201910207460 A CN 201910207460A CN 111717915 A CN111717915 A CN 111717915A
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Abstract
The invention relates to a method and a device capable of improving the capture rate of carbon dioxide in carbon dioxide flooding produced gas of an oil field, wherein the method comprises the following steps: pre-cooling the raw material gas; CO 22Cooling; carrying out flash separation on the raw material gas; low-temperature stripping; and recovering the overhead gas. The device includes: feed gas precooler, CO2The system comprises a cooler, a flash tank, a stripping tower, a tower bottom reboiler, a tower top cooler, a tower top gas separator, a tower top gas compressor and a compression outlet cooler; the tower bottom reboiler is connected with a feed gas precooler through a pipeline, and the feed gas precooler is connected with CO through a pipeline2Cooler connected to the CO2The cooler is connected with the flash tank through a pipeline, the flash tank is connected with the stripping tower through a pipeline, the stripping tower is connected with the tower top separator through a pipeline, and the tower top separator is connected with the tower top cooler through a pipeline. Compared with the prior cryogenic rectification processMainly develops a tower top gas recovery process, recycles cold quantity and realizes CO2The cyclic utilization of the catalyst reduces emptying and improves CO2The recovery rate of (1).
Description
Technical Field
The invention relates to the field of carbon dioxide separation and recovery, in particular to a method and a device capable of improving the capture rate of carbon dioxide in an oilfield carbon dioxide flooding produced gas.
Background
CO2Is a typical greenhouse gas, and CO is produced2The method is used for oil displacement of oil fields, can improve the recovery ratio of crude oil and can realize greenhouse gas CO2The permanent sealing of the container not only improves the economic benefit, but also generates wide social benefit. But utilizing CO in the oil field2Part of CO generated in oil-displacement process2Will be produced along with the oil gas production process, resulting in the produced gas containing a large amount of CO2The fraction of CO2Need to be collected and recycled, otherwise, the sealing effect and CO reduction are influenced2Environmental protection benefits are eliminated. The cryogenic rectification process is used for capturing CO2High concentration CO in the produced gas2The process can produce CO with high purity of over 96 percent2A liquid product; however, the process also has the disadvantages of low capture yield and CO2High emptying ratio and high unit trapping energy consumption, and reduces the CO content in the oil field2And (4) the benefit of driving and mining.
Disclosure of Invention
In view of the above, the present invention is to provide a high CO2The method and the device can improve the capture rate of the carbon dioxide in the carbon dioxide flooding produced gas of the oil field with low capture rate and low unit capture energy consumption.
In order to achieve the purpose, the method for improving the capture rate of the carbon dioxide in the produced gas of the carbon dioxide flooding of the oil field comprises the following steps:
1) pre-cooling the raw material gas;
2)CO2cooling;
3) carrying out flash separation on the raw material gas;
4) low-temperature stripping;
5) and recovering the overhead gas.
Further, the method for improving the capture rate of the carbon dioxide in the carbon dioxide flooding produced gas of the oil field comprises the following steps:
1) pre-cooling raw material gas: the dehydrated feed gas firstly passes through a tower bottom reboiler and then enters a feed gas precooler for cooling;
2)CO2and (3) cooling: then enters CO2The cooler is further cooled;
3) raw material gas flash separation: feeding the partially condensed feed gas in the step 2) into a flash tank for primary flash separation;
4) low-temperature stripping: the liquid phase obtained in the step 3) enters a stripping tower for purification, and liquid CO is obtained after purification2Producing a product;
5) recovering gas at the top of the tower: the gas at the top of the stripping tower is cooled by a tower top cooler and then enters a tower top separator to be separated into a liquid phase and a gas phase.
Further, the method for improving the capture rate of the carbon dioxide in the carbon dioxide flooding produced gas of the oil field comprises the following steps:
1) pre-cooling raw material gas: the raw material gas entering the device firstly passes through a reboiler at the bottom of the tower, simultaneously reduces the temperature of the raw material gas to 8 ℃, and then enters a raw material gas precooler for further precooling to 3-4 ℃;
2)CO2and (3) cooling: feeding the precooled feed gas into CO2The cooler is further cooled to-18 ℃ to-20 ℃ to partially condense the feed gas;
3) raw material gas flash separation: feeding the partially condensed feed gas in the step 2) into a flash tank for primary flash separation, and feeding the flash gas into a tower top gas recovery process;
4) low-temperature stripping: step 3), introducing the liquid phase separated by the flash tank into a stripping tower for purification, and purifying to obtain CO2Liquid CO with content of more than 99%2Producing a product;
5) recovering gas at the top of the tower:
the separated liquid phase is throttled and cooled, enters a tower top cooler to provide cold energy, then enters a precooler to exchange heat with the feed gas, enters a tower top gas compressor to be pressurized to the pressure of the feed gas entering the station after being heated, is cooled by a compression outlet cooler, then is merged with the feed gas and enters the subsequent flow again; the gas phase of the separator is throttled, depressurized and cooled, enters a cold box, then exchanges heat with the outlet gas of the tower top gas compressor to heat, and enters a fuel gas system to serve as fuel.
Further, the recovery of the overhead gas in the step 5) is specifically as follows: the gas phase of the stripping tower top gas and the flash tank gas phase are converged, and then the gas phase is cooled to-45 to-42 ℃ by a tower top cooler and enters a tower top gas separator to be separatedThrottling and cooling the coming liquid phase to-50-48 ℃, then entering a tower top cooler to provide cold energy, exchanging heat to-35-32 ℃, then entering a raw material gas precooler to exchange heat with the raw material gas and heating to 0-2 ℃, recycling the cold energy through the two-stage heat exchange, entering a tower top gas compressor to pressurize to the pressure of the raw material gas entering the station, cooling to 50 ℃ through a compression outlet cooler, then merging with the raw material gas and entering the subsequent flow again; the gas phase of the gas separator at the top of the tower contains 32 to 35 percent of CO2And the rest is hydrocarbon gas, the hydrocarbon gas is throttled, depressurized and cooled to-69 to-65 ℃, enters a tower top cooler to provide cold energy, is heated to-25 to-22 ℃, and then exchanges heat with gas at the outlet of a tower top gas compressor to heat to 10 to 13 ℃ to be used as fuel gas for self use in a station.
Further, wherein the feed gas to the unit in step 1) requires CO2The content is more than 70 percent, the water content is less than 200ppm, and the pressure is more than 3 MPa.
Further, in the step 4), the liquid phase separated by the flash tank in the step 3) contains heavy hydrocarbon and CO2。
The invention relates to a device capable of improving the capture rate of carbon dioxide in carbon dioxide flooding produced gas in an oil field, which is characterized by comprising the following components: feed gas precooler, CO2The system comprises a cooler, a flash tank, a stripping tower, a tower bottom reboiler, a tower top cooler, a tower top gas separator, a tower top gas compressor and a compression outlet cooler; the tower bottom reboiler is connected with a feed gas precooler through a pipeline, and the feed gas precooler is connected with CO through a pipeline2Cooler connected to the CO2The cooler is connected with the flash tank through a pipeline, the flash tank is connected with the stripping tower through a pipeline, the stripping tower is connected with the tower top separator through a pipeline, and the tower top separator is connected with the tower top cooler through a pipeline.
Further, the tower top cooler is respectively connected with the flash tank, the feed gas precooler and the compression outlet cooler through pipelines; the CO is2The cooler is also connected to the refrigeration unit.
Further, the overhead gas compressor is respectively connected with the feed gas precooler and the compression outlet cooler through pipelines.
Compared with the prior low-temperature rectification process, the process mainly develops a tower top gas recovery process, performs cold energy recovery and utilization, utilizes tower top noncondensable gas for self throttling refrigeration, enters a tower top cooler for providing cold energy for the tower top gas after throttling and cooling, and enters a precooler for precooling feed gas to further recover the cold energy after the tower top gas with the primary cold energy recovery; meanwhile, the tower top gas compressor pressurizes the tower top gas after recovering cold energy and returns the tower top gas to the feed gas inlet, thereby realizing CO2The cyclic utilization of the catalyst reduces emptying and improves CO2The collection rate of (1). The overhead gas recovery process developed by the invention is CO compared with the process before the addition2The trapping rate is improved by 10 percent, and the unit trapping energy consumption is reduced by about 7 percent.
Drawings
FIG. 1 is a schematic flow chart of the apparatus for increasing the capture rate of carbon dioxide in the carbon dioxide flooding produced gas in the oil field according to the present invention.
In the figure:
1-raw material gas precooler; 2-CO2A cooler; 3-a flash tank; 4-a stripping column; 5-a bottom reboiler; 6-overhead cooler; 7-a column top gas separator; 8-a top gas compressor; 9-compression outlet cooler.
Detailed Description
The present invention provides a method and apparatus for increasing the capture rate of carbon dioxide in the carbon dioxide-flooding produced gas of an oil field, and the following embodiments are provided for illustrative purposes only, and it should be understood that the embodiments described herein are not intended to limit the present invention.
As shown in fig. 1, the method for increasing the capture rate of carbon dioxide in the carbon dioxide flooding produced gas in the oil field provided by the invention comprises the following steps:
1) pre-cooling raw material gas: the raw material gas entering the device requires CO2Having a content of 90%, a water content of less than 200ppm and a pressure of 4MPa, is first passed through a bottom reboiler 5 to provide heat for the stripping operation (wherein liquid CO is present at the bottom of the column2External transportation), and simultaneously reducing the temperature of the feed gas to 8 ℃, and then entering a feed gas precooler 1 for further precooling to 4 ℃;
2)CO2and (3) cooling: feeding the precooled feed gas into CO2The cooler 2 is further cooled to-20 ℃ to condense about 80% of the feed gas into liquid, and the cold energy of the part is provided by the refrigerating unit, wherein the liquid ammonia entering the cooler comes from the refrigerating unit and cools CO by cooling2The formed gas ammonia returns to the refrigerating unit;
3) raw material gas flash separation: the partially condensed feed gas enters a flash tank 3 for primary flash separation, the flash gas enters a tower top gas recovery process, the flash gas in the feed gas is separated in advance and does not enter the tower, and the gas phase load at the tower top is reduced so as to reduce the gas phase load at the tower top;
4) low-temperature stripping: liquid phase (containing heavy hydrocarbons and CO) separated by flash drum2) Purifying in a stripping tower 4 to obtain CO2Liquid CO with content of more than 99%2Producing a product;
5) recovering gas at the top of the tower: the gas phase of the top gas of the stripping tower is converged with the gas phase of a flash tank, then the gas phase is cooled to minus 45 ℃ by a tower top cooler 6, then the gas phase enters a tower top gas separator 7, the separated liquid phase is throttled, the flash vaporization heat absorption of the liquid after throttling and pressure reduction is utilized to reduce the temperature to minus 50 ℃, then the liquid enters the tower top cooler 6 to provide cold energy, the cold energy is exchanged to minus 35 ℃, then the liquid enters a raw material gas precooler 1 to exchange heat with the raw material gas and raise the temperature to about 0 ℃, the cold energy is recycled by the two-stage heat exchange, the liquid enters a tower top gas compressor 8 to be pressurized to the raw material gas inlet pressure, the liquid is cooled to 50 ℃ by a compression outlet cooler 9 and then is converged with2The capture rate; the gas phase in the top gas separator 7 contains about 35% CO2The rest is hydrocarbon gas, the temperature is reduced to about minus 69 ℃ through throttling and pressure reduction, the hydrocarbon gas enters the tower top cooler 6 to provide cold energy, the temperature is raised to minus 25 ℃, and then the hydrocarbon gas exchanges heat with the gas at the outlet of the tower top gas compressor to heat to about 10 ℃, and the hydrocarbon gas is used as self-use fuel gas in the station.
As shown in fig. 1, the present invention also provides a device capable of increasing the capture rate of carbon dioxide in the carbon dioxide flooding produced gas in an oil field, comprising: feed gas precooler 1, CO2A cooler 2, a flash tank 3, a stripping tower 4, a tower bottom reboiler 5, a tower top cooler 6, a tower top gas separator 7 and a tower top gas pressureA compressor 8 and a compression outlet cooler 9; the tower bottom reboiler 5 is connected with the feed gas precooler 1 through a pipeline, and the feed gas precooler 1 is connected with CO through a pipeline2Cooler 2, the CO2The cooler 2 is connected with the flash tank 3 through a pipeline, the flash tank 3 is connected with the stripping tower 4 through a pipeline, the stripping tower 4 is connected with the tower top separator 7 through a pipeline, the tower top separator 7 is connected with the tower top cooler 6 through a pipeline, the tower top cooler 6 is respectively connected with the flash tank 3, the raw material gas precooler 1 and the compression outlet cooler 9 through pipelines, and the tower top gas compressor 8 is respectively connected with the raw material gas precooler 1 and the compression outlet cooler 9 through pipelines.
Furthermore, the CO2The cooler 2 is also connected to a refrigeration unit.
Due to CO in the feed gas of the above example2The content is 90%, and the others are hydrocarbon gases. In the conventional process, the energy consumption of pressurizing the raw material gas from 0.1MPa (the pressure of the produced gas is generally lower), the energy consumption of a refrigerating unit and the like are comprehensively considered, and CO is2The unit product energy consumption is 127.38kW.h/t, and after the tower top gas recovery flow of the invention is added, CO is obtained2The trapping rate is improved by 10 percent, the energy consumption of unit products is reduced to 117.67kW.h/t, and the energy consumption is reduced by about 7.63 percent.
The above examples are merely preferred embodiments for fully illustrating the present invention, and are not intended to limit the scope of the present invention. The equivalent substitution or change made by the technical personnel in the technical field on the basis of the invention is all within the protection scope of the invention. The scope of the present invention is defined by the claims.
Claims (9)
1. A method for improving the capture rate of carbon dioxide in the produced gas of carbon dioxide flooding in an oil field is characterized by comprising the following steps:
1) pre-cooling the raw material gas;
2)CO2cooling;
3) carrying out flash separation on the raw material gas;
4) low-temperature stripping;
5) and recovering the overhead gas.
2. The method for improving the capture rate of carbon dioxide in the carbon dioxide flooding produced gas in the oil field according to claim 1, which comprises the following steps:
1) pre-cooling raw material gas: the dehydrated feed gas firstly passes through a tower bottom reboiler and then enters a feed gas precooler for cooling;
2)CO2and (3) cooling: then enters CO2The cooler is further cooled;
3) raw material gas flash separation: feeding the partially condensed feed gas in the step 2) into a flash tank for primary flash separation;
4) low-temperature stripping: the liquid phase obtained in the step 3) enters a stripping tower for purification, and liquid CO is obtained after purification2Producing a product;
5) recovering gas at the top of the tower: the gas at the top of the stripping tower is cooled by a tower top cooler and then enters a tower top separator to be separated into a liquid phase and a gas phase.
3. The method for improving the capture rate of carbon dioxide in the carbon dioxide flooding produced gas in the oil field according to claim 2, which comprises the following steps:
1) pre-cooling raw material gas: 1) pre-cooling raw material gas: the raw material gas entering the device firstly passes through a reboiler at the bottom of the tower, simultaneously reduces the temperature of the raw material gas to 8 ℃, and then enters a raw material gas precooler for further precooling to 3-4 ℃;
2)CO2and (3) cooling: feeding the precooled feed gas into CO2The cooler is further cooled to-18 ℃ to-20 ℃ to partially condense the feed gas;
3) raw material gas flash separation: feeding the partially condensed feed gas in the step 2) into a flash tank for primary flash separation, and feeding the flash gas into a tower top gas recovery process;
4) low-temperature stripping: step 3), introducing the liquid phase separated by the flash tank into a stripping tower for purification, and purifying to obtain CO2Liquid CO with content of more than 99%2Producing a product;
5) recovering gas at the top of the tower:
the separated liquid phase is throttled and cooled, enters a tower top cooler to provide cold energy, then enters a precooler to exchange heat with the feed gas, enters a tower top gas compressor to be pressurized to the pressure of the feed gas entering the station after being heated, is cooled by an outlet cooler, then is merged with the feed gas and enters the subsequent flow again; the gas phase of the separator is throttled, depressurized and cooled, enters a cold box, then exchanges heat with the outlet gas of the tower top gas compressor to heat, and enters a fuel gas system to serve as fuel.
4. The method for improving the capture rate of the carbon dioxide in the carbon dioxide flooding produced gas in the oil field according to claim 3, wherein the recovery of the overhead gas in the step 5) is specifically as follows: after being converged with the gas phase of the flash tank, the gas at the top of the stripping tower is cooled to minus 45 ℃ to minus 42 ℃ by a tower top cooler and then enters a tower top gas separator, the separated liquid phase is throttled and cooled to minus 50 ℃ to minus 48 ℃, enters the tower top cooler to provide cold energy, is subjected to heat exchange to minus 35 ℃ to minus 32 ℃, then enters a raw material gas precooler to be subjected to heat exchange with raw material gas and heated to 0 ℃ to 2 ℃, is recycled with the cold energy through the two-stage heat exchange, enters a tower top gas compressor to be pressurized to the raw material gas inlet pressure, is cooled to 50 ℃ by a compression outlet cooler and then is converged with the raw material gas to enter the subsequent; the gas phase of the gas separator at the top of the tower contains 32 to 35 percent of CO2And the rest is hydrocarbon gas, the hydrocarbon gas is throttled, depressurized and cooled to-69 to-65 ℃, enters a tower top cooler to provide cold energy, is heated to-25 to-22 ℃, and then exchanges heat with gas at the outlet of a tower top gas compressor to heat to 10 to 13 ℃ to be used as fuel gas for self use in a station.
5. The method for improving the capture rate of carbon dioxide in the carbon dioxide flooding produced gas of the oil field according to any one of claims 1 to 4, wherein the raw gas fed into the device in the step 1) requires CO2The content is more than 70 percent, the water content is less than 200ppm, and the pressure is more than 3 MPa.
6. The method for improving the capture rate of the carbon dioxide in the carbon dioxide flooding produced gas of the oil field according to any one of claims 1 to 4, wherein in the step 4), the liquid phase separated from the flash tank in the step 3) contains heavy hydrocarbons and CO2。
7. The utility model provides a can improve device of carbon dioxide entrapment rate in oil field carbon dioxide flooding production gas which characterized in that includes: feed gas precooler, CO2The system comprises a cooler, a flash tank, a stripping tower, a tower bottom reboiler, a tower top cooler, a tower top gas separator, a tower top gas compressor and a compression outlet cooler; the tower bottom reboiler is connected with a feed gas precooler through a pipeline, and the feed gas precooler is connected with CO through a pipeline2Cooler connected to the CO2The cooler is connected with the flash tank through a pipeline, the flash tank is connected with the stripping tower through a pipeline, the stripping tower is connected with the tower top separator through a pipeline, and the tower top separator is connected with the tower top cooler through a pipeline.
8. The apparatus of claim 7 wherein the overhead cooler is connected by conduits to the flash drum, the feed gas precooler and the compression outlet cooler, respectively; the CO is2The cooler is also connected to the refrigeration unit.
9. The plant of claim 8 wherein the overhead gas compressor is connected by piping to the feed gas precooler and the compression outlet cooler, respectively.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114963691A (en) * | 2022-05-31 | 2022-08-30 | 山东石油化工学院 | Low pressure CO 2 Low-temperature gas separation method and device |
| CN115253585A (en) * | 2022-07-29 | 2022-11-01 | 中国科学院工程热物理研究所 | For CO2Method and system for utilizing collected residual pressure power generation cold energy |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176991A (en) * | 1996-08-28 | 1998-03-25 | 三菱重工业株式会社 | Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor |
| WO2009127440A1 (en) * | 2008-04-18 | 2009-10-22 | Institut Für Nachhaltigen Umweltschutz Inu Gbr | Method and device for separating carbon dioxide from stack, sludge, and/or exhaust gases |
| CN102853634A (en) * | 2012-08-14 | 2013-01-02 | 中国石油化工股份有限公司 | Method for recovering carbon dioxide |
| GB2493400A (en) * | 2011-08-05 | 2013-02-06 | Bp Alternative Energy Internat Ltd | Separation of carbon dioxide and hydrogen |
| CN205258018U (en) * | 2015-12-17 | 2016-05-25 | 江苏华扬液碳有限责任公司 | Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system |
| CN106440661A (en) * | 2016-08-31 | 2017-02-22 | 惠生工程（中国）有限公司 | Energy-saving type device for preparing high-purity liquid carbon dioxide and method |
| CN106440658A (en) * | 2016-09-27 | 2017-02-22 | 上海安恩吉能源科技有限公司 | Combination process for preparing liquefied natural gas (LNG) through high-oxygen-content and high-nitrogen-content coalbed methane |
| CN108641769A (en) * | 2018-06-05 | 2018-10-12 | 中国天辰工程有限公司 | A kind of recovery method of associated gas |
| CN108870868A (en) * | 2018-09-10 | 2018-11-23 | 江苏华扬液碳有限责任公司 | A kind of skid movable carbon dioxide displacement of reservoir oil output gas recovery system |
-
2019
- 2019-03-19 CN CN201910207460.4A patent/CN111717915B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176991A (en) * | 1996-08-28 | 1998-03-25 | 三菱重工业株式会社 | Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor |
| WO2009127440A1 (en) * | 2008-04-18 | 2009-10-22 | Institut Für Nachhaltigen Umweltschutz Inu Gbr | Method and device for separating carbon dioxide from stack, sludge, and/or exhaust gases |
| GB2493400A (en) * | 2011-08-05 | 2013-02-06 | Bp Alternative Energy Internat Ltd | Separation of carbon dioxide and hydrogen |
| CN102853634A (en) * | 2012-08-14 | 2013-01-02 | 中国石油化工股份有限公司 | Method for recovering carbon dioxide |
| CN205258018U (en) * | 2015-12-17 | 2016-05-25 | 江苏华扬液碳有限责任公司 | Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system |
| CN106440661A (en) * | 2016-08-31 | 2017-02-22 | 惠生工程（中国）有限公司 | Energy-saving type device for preparing high-purity liquid carbon dioxide and method |
| CN106440658A (en) * | 2016-09-27 | 2017-02-22 | 上海安恩吉能源科技有限公司 | Combination process for preparing liquefied natural gas (LNG) through high-oxygen-content and high-nitrogen-content coalbed methane |
| CN108641769A (en) * | 2018-06-05 | 2018-10-12 | 中国天辰工程有限公司 | A kind of recovery method of associated gas |
| CN108870868A (en) * | 2018-09-10 | 2018-11-23 | 江苏华扬液碳有限责任公司 | A kind of skid movable carbon dioxide displacement of reservoir oil output gas recovery system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114963691A (en) * | 2022-05-31 | 2022-08-30 | 山东石油化工学院 | Low pressure CO 2 Low-temperature gas separation method and device |
| CN114963691B (en) * | 2022-05-31 | 2023-12-26 | 山东石油化工学院 | Low pressure CO 2 Gas low-temperature separation method and device |
| CN115253585A (en) * | 2022-07-29 | 2022-11-01 | 中国科学院工程热物理研究所 | For CO2Method and system for utilizing collected residual pressure power generation cold energy |
| CN115253585B (en) * | 2022-07-29 | 2024-08-13 | 中国科学院工程热物理研究所 | For CO2Method and system for utilizing trapped residual pressure power generation cold energy |
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| CN111717915B (en) | 2022-02-01 |
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