CN115247083A - Graded gasification system and method - Google Patents
Graded gasification system and method Download PDFInfo
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- CN115247083A CN115247083A CN202211004535.7A CN202211004535A CN115247083A CN 115247083 A CN115247083 A CN 115247083A CN 202211004535 A CN202211004535 A CN 202211004535A CN 115247083 A CN115247083 A CN 115247083A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a staged gasification system and a staged gasification method, and relates to the technical field of coal gasification. The grading gasification system and the grading gasification method are used for grading raw coal in diameter dimension, a gasification furnace (a secondary gasification furnace) for coal dust with a smaller diameter adopts a smaller gasification wind speed, a gasification furnace (a primary gasification furnace) for coal dust with a larger diameter adopts a larger gasification wind speed, and in addition, solids (containing coal micro powder with the diameter of 20-100 um, wherein 100um is the diameter of the solid medium coal micro powder separated from the primary gasification furnace, and 20um is the diameter of the solid medium coal micro powder separated from the secondary gasification furnace) separated from outlets of the primary gasification furnace and the secondary gasification furnace continuously enter the secondary gasification furnace for continuous gasification reaction.
Description
Technical Field
The invention relates to the technical field of coal gasification, in particular to a staged gasification system and a staged gasification method.
Background
For a long time, the energy characteristics of China are rich coal, poor oil and less gas, and the clean and efficient utilization of coal becomes an important subject at present. The circulating fluidized bed gasification technology has the characteristics of wide raw material application range, high utilization efficiency, low device investment, cleanness, environmental protection and the like, and is popular in the fields of fuel gas and medium and small coal chemical industry in China.
Because the circulating fluidized bed gasification furnace adopts a solid slag discharging mode, the gasification temperature is generally required to be 150-200 ℃ lower than the softening temperature of the melting point of coal ash. Considering the influence of the reactivity and ash fusion point of coal, the operation temperature of the circulating fluidized bed gasification furnace is generally 900-1000 ℃.
The prior fluidized bed technology adopts a wide distribution form that raw coal particles are distributed in a size of 0-10 mm, and raw coal is generally directly crushed and then is sent to a circulating fluidized bed gasification furnace for gasification at a certain fluidization air speed; therefore, fine powdered coal is blown out of the hearth without reacting with the gasifying agent in the hearth and continuously participating in the reaction, the powdered coal is only subjected to the devolatilization process in the gas furnace, and the carbon content of the fly ash of the existing fluidized bed gasification furnace is generally over 70 percent.
Therefore, the invention aims to develop a graded gasification method, solve the problems of large fly ash amount and high fly ash carbon content of the existing circulating fluidized bed gasification furnace and realize clean and efficient utilization of coal.
Disclosure of Invention
Technical problem to be solved
Aiming at the defects of the prior art, the invention provides a graded gasification system and a graded gasification method, which solve the following technical problems:
due to the fact that the particle size distribution of raw coal particles is wide, coal powder with smaller particles can directly enter a subsequent dust removal link at a high fluidization air speed, and further carbon content in fly ash is high.
(II) technical scheme
In order to achieve the purpose, the invention is realized by the following technical scheme: a graded gasification system is used for graded gasification of coal particles and gasifying agents in different particle size ranges and comprises a primary gasification furnace and a secondary gasification furnace, wherein the coal particles comprise fine coal particles and coarse coal particles, and the particle size of the fine coal particles is smaller than that of the coarse coal particles;
the primary gasification furnace is used for gasifying coarse coal particles;
the secondary gasification furnace is used for gasifying fine coal particles;
the outlet of the primary gasification furnace is connected with a primary solid-gas separator;
the outlet of the secondary gasification furnace is connected with a secondary solid-gas separator;
the solid discharge outlet of the primary solid-gas separator is connected with the secondary gasification furnace;
the solid discharge outlet of the secondary solid-gas separator is connected with the secondary gasification furnace;
the fluidization air speed of the reaction section in the primary gasification furnace is higher than that of the reaction section in the secondary gasification furnace;
the coarse coal particles in the primary gasification furnace are dragged by high-speed airflow to be in a suspension state and react with a gasification agent;
the carbon content of the fly ash in the primary solid-gas separator and the secondary solid-gas separator is less than 40% of the mass of the fly ash.
Preferably, the diameter of the fine coal particles is in the range of 0 to 5 mm.
Preferably, the diameter of the fine coal particles is in the range of 0 to 3 mm.
Preferably, the reaction section of the primary gasification furnace adopts a high-speed fluidization mode, and the fluidization air speed of the reaction section in the primary gasification furnace is A-Bm/s.
Preferably, the fluidizing air speed of the reaction section in the secondary gasifier is 0.06A-0.07 Bm/s.
Preferably, the fluidizing air speed of the reaction section in the secondary gasifier is 0.04A-0.07 Bm/s.
Preferably, the fluidizing air speed of the reaction section in the secondary gasification furnace is 0.06A-0.1 Bm/.
Preferably, the fluidizing air speed of the reaction section in the secondary gasifier is 0.04A-0.1 Bm/.
Preferably, the reaction temperature in the primary gasification furnace is 970-1000 ℃.
Preferably, the reaction temperature in the secondary gasification furnace is 950 ℃ to 970 ℃.
A staged gasification method for staged gasification of coal particles and gasification agents with different particle size ranges comprises a staged gasification system and the following steps:
the coarse coal particles enter a first-stage gasification furnace to carry out gasification reaction with a gasification agent, reaction products are subjected to solid-gas separation through a first-stage solid-gas separator, and the separated solids enter a second-stage gasification furnace to carry out gasification reaction with the gasification agent;
the fine coal particles enter a secondary gasification furnace to carry out gasification reaction with a gasification agent, the reaction product is subjected to solid-gas separation through a secondary solid-gas separator, and the separated solid enters the secondary gasification furnace again to carry out gasification reaction with the gasification agent.
Preferably, the raw coal is screened by the screen, fine coal particles pass through the screen, raw coarse coal particles pass through the screen, and the raw coarse coal particles are crushed by the crusher to obtain coarse coal particles.
(III) advantageous effects
The invention provides a staged gasification system and a staged gasification method. The method has the following beneficial effects:
the grading gasification system and the grading gasification method are used for grading raw coal in diameter dimension, a gasification furnace (a secondary gasification furnace) for coal dust with a smaller diameter adopts a smaller gasification wind speed, a gasification furnace (a primary gasification furnace) for coal dust with a larger diameter adopts a larger gasification wind speed, and in addition, solids (containing coal micro powder with the diameter of 20-100 um, wherein 100um is the diameter of the solid medium coal micro powder separated from the primary gasification furnace, and 20um is the diameter of the solid medium coal micro powder separated from the secondary gasification furnace) separated from outlets of the primary gasification furnace and the secondary gasification furnace continuously enter the secondary gasification furnace for continuous gasification reaction.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1:
the raw coal is conveyed to a roller screen for screening through a conveyor in a raw coal storage yard, and the screened fine coal particles with the particle size of 0-5 mm are conveyed to a fine coal hopper. And conveying the screened coarse particles to a crusher for crushing through a conveyor, and conveying generated coal particles with the size of 5-10 mm to a coarse coal hopper. Coarse coal particles of 5-10 mm are sent to a first-stage gasification furnace for gasification. The reaction section of the first-stage gasification furnace adopts a high-speed fluidization mode, the fluidization air speed of the reaction section is 5-10 m/s, large-particle coal powder in the first-stage gasification furnace is in a suspension state under the dragging of high-speed airflow and reacts violently with a gasification agent, and the reaction temperature of the first-stage gasification furnace is 970-1000 ℃. Gas and solid separation is carried out on the coal gas and the fly ash generated from the first-stage gasification furnace through a first-stage separator, and the separated solid particles are sent to the second-stage gasification furnace through a screw feeder.
The fine coal particles with the diameter of 0-5 mm in the fine coal hopper enter a secondary gasification furnace and are gasified in the secondary gasification furnace with the material separated by a primary separator, the fluidization air speed of the reaction section of the secondary gasification furnace is 0.3-1 m/s, and the reaction temperature of the secondary gasification furnace is 950-970 ℃. And carrying out gas-solid separation on the dust-containing gas generated by gasification of the secondary gasification furnace through a secondary separator, mixing the dust-containing gas with the gas of the primary separator, and then cooling.
Example 2:
the raw coal is conveyed to a roller screen for screening through a conveyor in a raw coal storage yard, and the screened fine coal particles with the particle size of 0-3 mm are conveyed to a fine coal hopper. And conveying the screened coarse particles to a crusher through a conveyor for crushing to generate coal particles of 3-10 mm, and conveying the coal particles to a coarse coal hopper. Coarse coal particles of 3-10 mm are sent to a first-stage gasification furnace for gasification. The reaction section of the first-stage gasification furnace adopts a high-speed fluidization mode, the fluidization air speed of the reaction section is 5-7 m/s, large-particle coal powder in the first-stage gasification furnace is in a suspension state under the dragging of high-speed airflow and reacts violently with a gasification agent, and the reaction temperature of the first-stage gasification furnace is 970-1000 ℃. Gas and solid separation is carried out on the coal gas and the fly ash generated from the first-stage gasification furnace through a first-stage separator, and the separated solid particles are sent to the second-stage gasification furnace through a screw feeder.
The fine coal particles with the diameter of 0-3 mm in the fine coal hopper enter a secondary gasification furnace and are gasified with the material separated by a primary separator in the secondary gasification furnace, the fluidization air speed of the reaction section of the secondary gasification furnace is 0.3-0.5 m/s, and the reaction temperature of the secondary gasification furnace is 950-970 ℃. And carrying out gas-solid separation on the dust-containing gas generated by gasification of the secondary gasification furnace through a secondary separator, mixing the dust-containing gas with the gas of the primary separator, and then cooling.
Comparative example 1:
the difference from example 1 is that: the raw coal is crushed by a crusher and then enters a primary reaction furnace for reaction.
Comparative example 2:
the difference from example 1 is that: the solid material separated by the first-stage separator does not enter the second-stage gasification furnace, but directly enters the dust removal system (after passing through the heat exchange system).
Comparative example 3:
the difference from example 1 is that: the solid material separated by the secondary separator does not enter the secondary gasification furnace, but directly enters the dust removal system (after passing through the heat exchange system).
Comparative example 4:
the difference from example 1 is that: the solid material separated by the first-stage separator and the solid material separated by the second-stage separator do not enter the second-stage gasification furnace, but directly enter the dust removal system (after passing through the heat exchange system).
Comparative example 5:
the difference from example 1 is that:
the fluidization wind speed of the secondary gasification furnace is 0.6-2 m/s.
Comparative example 6:
the difference from example 1 is that:
the fluidization wind speed of the secondary gasification furnace is 0.9-3 m/s.
Comparative example 7:
the difference from example 1 is that:
the fluidization wind speed of the secondary gasification furnace is 0.2-0.29 m/s.
The following table shows the carbon content in fly ash of the final separator in each of examples and comparative examples.
Note: the fly ash in the carbon content of the fly ash is the fly ash before entering the dust removal system.
The difference between example 1 and example 2 is that the wind speed and the particle size are different, and it can be seen that the matching of the wind speed is smaller when the particle size in the secondary gasifier is smaller (0-3 mm), and the particle size in the primary gasifier is also smaller (3-5 mm), so the primary gasifier fluidization wind speed and the secondary gasifier fluidization wind speed in example 2. However, the initial particle size selection range is smaller, resulting in a higher carbon content in the final fly ash than in the fly ash of example 1.
Comparative example 1 differs from example 1 in that there is no secondary gasification system (prior art non-staged gasification system), and it can be seen that the carbon content in fly ash is up to 70% with all other parameters being the same. It can also be seen that the carbon content in the fly ash can be effectively reduced by adopting the two-stage gasification system in the embodiment 1. The reason why the carbon content of the fly ash of example 1 is reduced is not that the proportion of the ash is increased but that the carbon content of the ash is effectively reduced. The total amount of fly ash was also reduced in example 1 compared to comparative example 1.
Comparative example 2 is different from example 1 in that the solids separated in the primary separator are not recovered and the carbon content of fly ash is reduced compared to comparative example 1.
Comparative example 3 is different from example 1 in that the solids separated in the second stage separator are not recovered and the carbon content of fly ash is reduced compared to comparative example 1.
The technical solution of example 1 is equal to comparative example 2 plus comparative example 3 to some extent, but actually, the technical effect of example 1 is obviously better than the sum of the technical effects of comparative example 2 and comparative example 3 (compared with comparative example 1, the carbon content of the fly ash of comparative example 2 is reduced by 5%, the carbon content of the fly ash of comparative example 3 is reduced by 7%, the total carbon content is reduced by 12%, and the carbon content of the fly ash of example 1 is reduced by 36%), because the two or three comparative examples are based on comparative example 1, but comparative example 2 does not recover the primary separator. Comparative example 3 was not recovered by two-stage separation. The action of the separator can lead the collected fly ash to circularly enter the hearth for reacting for many times, thereby greatly reducing the carbon content. In both comparative examples 2 and 3, a large amount of fly ash was not reacted and directly discharged, resulting in an increase in carbon content. In the embodiment 1, the fly ash in the whole system is separated and circulated by the separator to participate in the reaction, the particle circulation time is long, and the reaction is sufficient, so that the aim of high carbon conversion rate is fulfilled.
Comparative example 4 is different from example 1 in that the solids separated by the separators (the first stage separator and the second stage separator) were not recovered, and the carbon content of fly ash was equivalent to that in comparative example 1 when the solid material separated by the first stage separator and the solid material separated by the second stage separator were not recovered.
The difference between the comparative example 5 and the example 1 is that the fluidizing air speed of the secondary gasification furnace is twice of that of the example 1, and the fine coal dust particles can directly enter the dust removal system without reacting in the gasification furnace under the condition of large air speed adjustment, so that the carbon content in the fly ash is increased.
The difference between comparative example 6 and example 1 is that the fluidizing air velocity of the secondary gasification furnace is three times that of example 1, and further increase of the air velocity results in further increase of the carbon content in fly ash.
The difference between the comparative example 7 and the example 1 is that the fluidizing air speed of the secondary gasification furnace is lower than the air speed corresponding to the example 1, and the comparative example 7 also achieves the better effect of reducing the carbon content of the fly ash, but because the fluidizing air speed of the secondary gasification furnace is lower, the inner wall and the pipeline of the secondary gasification furnace are easy to coke, and further the stability of the system operation is caused.
In summary, the staged gasification system and method perform staged treatment on raw coal in diameter dimension, a gasification furnace (secondary gasification furnace) for pulverized coal with a smaller diameter adopts a smaller gasification air speed, a gasification furnace (primary gasification furnace) for pulverized coal with a larger diameter adopts a larger gasification air speed, and solids (containing coal fines with diameters of 20-100 um, wherein 100um is the diameter of the solid medium-coal fines separated from the primary gasification furnace, and 20um is the diameter of the solid medium-coal fines separated from the secondary gasification furnace) separated from outlets of the primary gasification furnace and the secondary gasification furnace continuously enter the secondary gasification furnace to perform gasification reaction continuously.
It should be noted that in the description of the present invention, the terms "upper", "lower", "left", "right", "front", "rear", and the like indicate orientations or positional relationships based on structures shown in the drawings, and are only used for convenience in describing the present invention, but do not indicate or imply that the referred devices or elements must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
The terms "first" and "second" in the present technical solution are only used to distinguish the same or similar structures or the corresponding structures having similar functions, and are not the arrangement of the importance of the structures, nor are they the order, or comparison of the sizes, or other meanings.
In addition, unless expressly stated or limited otherwise, the terms "mounted" and "connected" are to be construed broadly, e.g., the connection may be a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; the two structures can be directly connected or indirectly connected through an intermediate medium, and the two structures can be communicated with each other. To those skilled in the art, the specific meanings of the above terms in the present invention can be understood in light of the present general concepts, in connection with the specific context of the scheme.
Claims (10)
1. The utility model provides a hierarchical gasification system for the hierarchical gasification of coal particle and gasifying agent of different particle diameter scopes, including one-level gasifier, second grade gasifier, its characterized in that: the coal particles comprise fine coal particles and coarse coal particles, and the particle size of the fine coal particles is smaller than that of the coarse coal particles;
the primary gasification furnace is used for gasifying coarse coal particles;
the secondary gasification furnace is used for gasifying fine coal particles;
the outlet of the primary gasification furnace is connected with a primary solid-gas separator;
the outlet of the secondary gasification furnace is connected with a secondary solid-gas separator;
the solid discharge outlet of the primary solid-gas separator is connected with the secondary gasification furnace;
the solid discharge outlet of the secondary solid-gas separator is connected with the secondary gasification furnace;
the fluidization air speed of the reaction section in the primary gasification furnace is higher than that of the reaction section in the secondary gasification furnace;
the coarse coal particles in the primary gasification furnace are dragged by high-speed airflow to be in a suspension state and react with a gasification agent;
the carbon content of the fly ash in the primary solid-gas separator and the secondary solid-gas separator is less than 40% of the mass of the fly ash.
2. The staged gasification system of claim 1, wherein: the diameter of the fine coal particles is in the range of 0 to 5 mm.
3. The staged gasification system of claim 1, wherein: the diameter of the fine coal particles is within the range of 0-3 mm.
4. The staged gasification system of claim 1, wherein: the reaction section of the primary gasification furnace adopts a high-speed fluidization mode, and the fluidization air speed of the reaction section in the primary gasification furnace is A-Bm/s.
5. The staged gasification system of claim 4, wherein: the fluidization air speed of the reaction section in the secondary gasification furnace is 0.06A-0.07 Bm/s.
6. The staged gasification system of claim 4, wherein: the fluidization air speed of the reaction section in the secondary gasification furnace is 0.06A-0.1 Bm/s.
7. The staged gasification system of claim 1, wherein: the reaction temperature in the primary gasification furnace is 970-1000 ℃.
8. The staged gasification system of claim 1, wherein: the reaction temperature in the secondary gasification furnace is 950-970 ℃.
9. A graded gasification method is used for graded gasification of coal particles and gasification agents with different particle size ranges, and is characterized in that: comprising a staged gasification system according to claim 1 and the steps of:
the coarse coal particles enter a first-stage gasification furnace to carry out gasification reaction with a gasification agent, reaction products are subjected to solid-gas separation through a first-stage solid-gas separator, and the separated solids enter a second-stage gasification furnace to carry out gasification reaction with the gasification agent;
the fine coal particles enter a secondary gasification furnace to carry out gasification reaction with a gasification agent, the reaction product is subjected to solid-gas separation through a secondary solid-gas separator, and the separated solid enters the secondary gasification furnace again to carry out gasification reaction with the gasification agent.
10. A staged gasification process according to claim 9, wherein: the raw coal is screened by the screen, fine coal particles pass through the screen, raw coarse coal particles pass through the screen, and the raw coarse coal particles are crushed by the crusher to obtain coarse coal particles.
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