A zero-carbon coke making system and method

Abstract

The present application provides a zero-carbon emission coking system and coking method, the coking system comprises a coking furnace, a secondary combustion furnace, an adsorption tower, an active coke adsorber and a regeneration tower, the coking furnace, the secondary combustion furnace, the adsorption tower and the active coke adsorber are connected in sequence, the rich liquid outlet of the adsorption tower is connected with the rich liquid inlet of the regeneration tower to regenerate the rich liquid, the obtained lean liquid is returned to the adsorption tower for reuse, the lean liquid and the rich liquid exchange heat through a heat exchanger during transmission, and the carbon dioxide discharged from the regeneration tower is transported back to the coking furnace as an activating agent to participate in the preparation of active coke. The present application realizes complete capture of CO2 discharged in the coking process and realizes zero-carbon emission in the coking process. The present application uses the captured CO2 as an activating agent for preparing active coke, has good adsorption performance for small molecules, and improves the yield of active coke. The present application can realize the heat cascade utilization of the system, and effectively reduces the heat consumption of the regeneration process.

Description

Technical Field

[0001] This invention relates to the field of activated coke preparation, and more particularly to a zero-carbon emission coking system and coking method. Background Technology

[0002] The production of activated coke from raw coal involves carbonization and activation, ultimately forming a highly porous structure. The yield from raw material to product in activated coke production is only 30%–50%, with the remaining components of the coal being burned and emitted during the coking process, causing significant carbon emissions. While organic amine flue gas carbon dioxide capture technology is relatively mature and can completely remove CO2 from flue gas, it currently suffers from high energy consumption during carbon capture and regeneration, and low utilization rate of captured CO2. The high energy consumption is primarily due to the need for thermal regeneration after the organic amine adsorbent becomes saturated with captured CO2. This thermal regeneration process consumes a large amount of energy, accounting for over 70% of the total operating energy consumption, resulting in high costs for carbon capture. Currently, the captured CO2 is used for geological storage and industrial processing, with low utilization rates, failing to achieve high-value-added utilization. Summary of the Invention

[0003] The present invention aims to at least partially solve one of the technical problems in the related art. To this end, the embodiments of the present invention provide a zero-carbon emission coking system that completely captures CO2 emitted during the coking process, thereby achieving zero carbon emissions during the coking process. Furthermore, the captured CO2 is used as an activation gas in the coking process, thereby improving the utilization rate of the captured CO2 and reducing regeneration energy consumption.

[0004] One embodiment of the present invention proposes a zero-carbon emission coking system, comprising: a coking oven, a secondary combustion oven, an adsorption tower, an activated coke adsorber, and a regeneration tower. The coking oven has a first flue gas outlet and a coking oven carbon dioxide inlet. The shell side of the secondary combustion oven has a first flue gas inlet and a second flue gas outlet, and the tube side of the secondary combustion oven has a combustion oven carbon dioxide inlet and a carbon dioxide outlet. The first flue gas outlet is connected to the first flue gas inlet, and the carbon dioxide outlet is connected to the coking oven carbon dioxide inlet.

[0005] The adsorption tower has a second flue gas inlet, a third flue gas outlet, a rich liquid outlet, and a lean liquid inlet, with the second flue gas outlet connected to the second flue gas inlet; the activated coke adsorber has a third flue gas inlet and a clean flue gas outlet, with the third flue gas inlet connected to the third flue gas outlet; the regeneration tower has a first regeneration tower rich liquid inlet, a regeneration tower lean liquid outlet, and a carbon dioxide emission port, with the first regeneration tower rich liquid inlet connected to the adsorption tower rich liquid outlet via a first pipeline, and the regeneration tower lean liquid outlet connected to the adsorption tower lean liquid inlet via a second pipeline, the first pipeline and the second pipeline being connected via a first heat exchanger for heat exchange between the media in the first pipeline and the second pipeline, and the carbon dioxide emission port connected to the carbon dioxide inlet of the combustion furnace.

[0006] The inventors discovered through research that existing coking systems mostly use steam activation or flue gas (H2O, CO2, O2) activation. The activation reaction is intense, causing the micropores created by the activator etching to collapse and the mesopores to enlarge. This results in activated coke with low micropore content, a high proportion of mesopores and macropores, poor strength, and weak adsorption capacity for small molecules. Furthermore, the intense etching reaction between the activator (steam or flue gas) and the raw materials leads to a low yield of activated coke, only 30%–50%.

[0007] This application uses captured CO2 as an activator in the preparation of activated carbon. The prepared activated carbon has a well-developed and strong microporous structure, exhibiting good adsorption performance for small molecules. The activation reaction rate is controllable, increasing the yield of activated carbon to over 50%, while also improving the utilization rate of captured CO2.

[0008] This application combines a coking system with a carbon capture system to achieve complete capture of CO2 emitted during the coking process, thus achieving zero carbon emissions during the coking process.

[0009] This application adds an activated coke adsorber after the adsorption tower to effectively adsorb the volatile organic amines released during the flue gas purification process, preventing the organic amines from being released into the atmosphere after decarbonization, which would cause serious environmental problems, increase volatile organic compounds, and generate toxic and carcinogenic substances such as nitrosamines in the atmosphere, resulting in secondary pollution.

[0010] This application enables the cascade utilization of system heat by setting up a heat exchanger, effectively reducing the heat consumption during the regeneration process.

[0011] In some embodiments, the zero-carbon emission coking system further includes a second heat exchanger. The tube side of the second heat exchanger is connected to a pipeline connecting the second flue gas outlet and the second flue gas inlet. The regeneration tower also has a rich liquor outlet and a rich liquor inlet. The shell side of the second heat exchanger is connected to the rich liquor outlet and the rich liquor inlet of the regeneration tower via pipelines, respectively. The rich liquor is heated to above 120°C using the second heat exchanger to obtain lean liquor and carbon dioxide.

[0012] This application utilizes the high-temperature flue gas generated during the coking process as a regeneration heat source for the organic amine adsorbent, which enables the cascade utilization of system heat and effectively reduces the heat consumption during the regeneration process.

[0013] In some embodiments, the zero-carbon emission coking system further includes a dust collector connected to a pipeline connecting the second flue gas outlet of the secondary combustion furnace and the second flue gas inlet of the adsorption tower. The dust collector removes particulate matter from the high-temperature flue gas.

[0014] In some embodiments, the dust collector is located between the second heat exchanger and the adsorption tower.

[0015] In some embodiments, the zero-carbon emission coking system further includes an induced draft fan, which is installed on the pipeline connecting the dust collector and the second flue gas inlet of the adsorption tower. The induced draft fan provides power for the transport of the flue gas.

[0016] In some embodiments, the coking oven includes: a carbonization section, an activation section, and a cooling section. The carbonization section has a first furnace chamber and a feed inlet, a first outlet, and a first flue gas outlet connected to the first furnace chamber. The activation section has a second furnace chamber and a second outlet connected to the second furnace chamber and a carbon dioxide inlet for the coking oven. The second furnace chamber is connected to the first furnace chamber through the first outlet. The cooling section has a third furnace chamber and a third outlet connected to the third furnace chamber. The third furnace chamber is connected to the second furnace chamber through the second outlet. The third furnace chamber is equipped with a cooling device.

[0017] In some embodiments, a rich solution pump is connected to the pipeline between the rich solution outlet of the adsorption tower and the rich solution inlet of the first regeneration tower, and a lean solution pump is connected to the pipeline between the lean solution outlet of the regeneration tower and the lean solution inlet of the adsorption tower. The rich solution pump and the lean solution pump provide power for the transport of the rich and lean solutions.

[0018] Another embodiment of the present invention proposes a zero-carbon emission coking method, utilizing the aforementioned zero-carbon emission coking system, comprising the following steps: The flue gas generated during the coking process in the coking oven enters a secondary combustion furnace for combustion, yielding high-temperature flue gas; the high-temperature flue gas, after cooling and dust removal, enters an adsorption tower for adsorption to remove carbon dioxide, yielding amine-containing flue gas; the amine-containing flue gas enters an activated coke adsorber to adsorb the organic amines in the flue gas, yielding clean flue gas, which is then discharged into the atmosphere; the rich liquor saturated in the adsorption tower enters a regeneration tower for regeneration; the lean liquor obtained after regeneration enters the adsorption tower for reuse; the carbon dioxide generated during the regeneration process in the regeneration tower is used as an activation gas to participate in the activation section of the coking oven in the preparation of activated coke.

[0019] This application uses captured CO2 as an activator in the preparation of activated carbon. The prepared activated carbon has a well-developed and strong microporous structure, exhibiting good adsorption performance for small molecules. The activation reaction rate is controllable, increasing the yield of activated carbon to over 50%, while also improving the utilization rate of captured CO2.

[0020] This application combines a coking system with a carbon capture system to achieve complete capture of CO2 emitted during the coking process, thus achieving zero carbon emissions during the coking process.

[0021] This application adds an activated coke adsorber after the adsorption tower to effectively adsorb the volatile organic amines released during the flue gas purification process, preventing the organic amines from being released into the atmosphere after decarbonization, which would cause serious environmental problems, increase volatile organic compounds, and generate toxic and carcinogenic substances such as nitrosamines in the atmosphere, resulting in secondary pollution.

[0022] In some embodiments, the adsorption-saturated rich liquid discharged from the adsorption tower enters the regeneration tower after passing through the first heat exchanger, and the higher-temperature regenerated lean liquid discharged from the regeneration tower enters the adsorption tower after exchanging heat with the lower-temperature adsorption-saturated rich liquid in the first heat exchanger.

[0023] In some embodiments, the system further includes a second heat exchanger and a dust collector. The adsorption-saturated rich liquid in the regeneration tower is passed into the second heat exchanger for heat exchange and temperature increase, and the resulting lean liquid and carbon dioxide are returned to the regeneration tower. The high-temperature flue gas discharged from the secondary combustion furnace is cooled by heat exchange with the adsorption-saturated rich liquid in the second heat exchanger. The cooled flue gas enters the dust collector for dust removal and then enters the adsorption tower to remove carbon dioxide. Attached Figure Description

[0024] The above and / or additional aspects and advantages of the present invention will become apparent and readily understood from the following description of the embodiments taken in conjunction with the accompanying drawings.

[0025] in:

[0026] Figure 1 This is a schematic diagram of the zero-carbon emission coking system in the embodiments of this application;

[0027] Figure label:

[0028] 1-Coking oven, 101-Carbonization section, 102-Activation section, 103-Cooling section, 2-Secondary combustion furnace, 3-Second heat exchanger, 4-Dust collector, 5-Induced draft fan, 6-Adsorption tower, 7-Activated coke adsorber, 8-Rich liquor pump, 9-First heat exchanger, 10-Lean liquor pump, 11-Regeneration tower. Detailed Implementation

[0029] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0030] The zero-carbon emission coking system of the present invention is described below with reference to the accompanying drawings.

[0031] like Figure 1 As shown, one embodiment of this application proposes a zero-carbon emission coking system, including: a coking oven 1, a secondary combustion furnace 2, an adsorption tower 6, an activated coke adsorber 7, and a regeneration tower 11. The coking oven 1 has a first flue gas outlet and a coking oven carbon dioxide inlet; the shell side of the secondary combustion furnace 2 has a first flue gas inlet and a second flue gas outlet, and the tube side of the secondary combustion furnace 2 has a combustion furnace carbon dioxide inlet and a carbon dioxide outlet. The first flue gas outlet is connected to the first flue gas inlet, and the carbon dioxide outlet is connected to the coking oven carbon dioxide inlet.

[0032] The adsorption tower 6 has a second flue gas inlet, a third flue gas outlet, a rich liquid outlet, and a lean liquid inlet, with the second flue gas outlet connected to the second flue gas inlet; the activated coke adsorber 7 has a third flue gas inlet and a clean flue gas outlet, with the third flue gas inlet connected to the third flue gas outlet; the regeneration tower 11 has a first regeneration tower rich liquid inlet, a regeneration tower lean liquid outlet, and a carbon dioxide emission port, with the first regeneration tower rich liquid inlet connected to the adsorption tower rich liquid outlet via a first pipeline, and the regeneration tower lean liquid outlet connected to the adsorption tower lean liquid inlet via a second pipeline, the first pipeline and the second pipeline being connected via a first heat exchanger 9 for heat exchange of the media in the first pipeline and the second pipeline, and the carbon dioxide emission port being connected to the carbon dioxide inlet of the combustion furnace.

[0033] The inventors discovered through research that existing coking systems mostly use steam activation or flue gas (H2O, CO2, O2) activation. The activation reaction is intense, causing the micropores created by the activator etching to collapse and the mesopores to enlarge. This results in activated coke with low micropore content, a high proportion of mesopores and macropores, poor strength, and weak adsorption capacity for small molecules. Furthermore, the intense etching reaction between the activator (steam or flue gas) and the raw materials leads to a low yield of activated coke, only 30%–50%.

[0034] This application uses captured CO2 as an activator in the preparation of activated carbon. The prepared activated carbon has a well-developed and strong microporous structure, exhibiting good adsorption performance for small molecules. The activation reaction rate is lower than that of water vapor, and the activation reaction rate is controllable. CO2 undergoes a non-uniform activation reaction with carbon microcrystals, forming a large number of micropores on the carbon microcrystals. This prevents the vigorous activation reaction of water vapor from causing the micropores to enlarge or merge, forming mesopores and macropores.

[0035] The activated carbon obtained in this application has increased the yield to more than 50%, while also improving the utilization rate of captured CO2.

[0036] The coking process involves the carbonization and activation of coal particles. Amorphous carbon and volatile matter in the coal decompose upon heating, ultimately being emitted as CO2, resulting in substantial carbon emissions during coking. This application combines a coking system with a carbon capture system to achieve complete CO2 capture during the coking process, thus realizing zero carbon emissions.

[0037] This application adds an activated coke adsorber 7 after the adsorption tower 6 to effectively adsorb the volatile organic amines during the flue gas purification process, preventing the organic amines from being released into the atmosphere after decarbonization, which would cause serious environmental problems, increase volatile organic compounds, and generate toxic and carcinogenic substances such as nitrosamines in the atmosphere, resulting in secondary pollution.

[0038] This application enables the cascade utilization of system heat by setting up a heat exchanger, effectively reducing the heat consumption during the regeneration process.

[0039] It is understandable that rich solution can be understood as adsorbent that has reached adsorption saturation, and lean solution can be understood as adsorbent after regeneration.

[0040] Furthermore, the first heat exchanger 9 is a lean liquid-rich liquid heat exchanger, which transfers the heat of the regenerated lean liquid to the rich liquid to preheat the rich liquid, so that the heat consumption of the rich liquid can be reduced when it enters the regeneration tower 11.

[0041] Furthermore, the carbon dioxide emission outlet is located at the top of the regeneration tower 11.

[0042] In some embodiments, the zero-carbon emission coking system further includes a second heat exchanger 3. The tube side of the second heat exchanger 3 is connected to a pipeline connecting the second flue gas outlet and the second flue gas inlet. The regeneration tower 11 also has a rich liquor outlet and a rich liquor inlet. The shell side of the second heat exchanger 3 is connected to the rich liquor outlet and the rich liquor inlet of the regeneration tower via pipelines, respectively. The rich liquor is heated to above 120°C using the second heat exchanger 3 to obtain lean liquor and carbon dioxide.

[0043] This application utilizes the high-temperature flue gas generated during the coking process as a regeneration heat source for the organic amine adsorbent, which enables the cascade utilization of system heat and effectively reduces the heat consumption during the regeneration process.

[0044] Furthermore, the second heat exchanger 3 is a regeneration fluidizer. The rich liquid outlet of the regeneration tower is located at the bottom of the regeneration tower 11, and the rich liquid inlet of the second regeneration tower is located near the middle of the regeneration tower 11.

[0045] In some embodiments, the zero-carbon emission coking system further includes a dust collector 4, which is connected to the pipeline connecting the second flue gas outlet of the secondary combustion furnace 2 and the second flue gas inlet of the adsorption tower 6. The dust collector 4 removes particulate matter from the high-temperature flue gas.

[0046] In some embodiments, the dust collector 4 is disposed between the second heat exchanger 3 and the adsorption tower 6.

[0047] In some embodiments, the zero-carbon emission coking system further includes an induced draft fan 5, which is installed on the pipeline connecting the dust collector 4 and the second flue gas inlet of the adsorption tower 6. The induced draft fan 5 provides power for the transport of flue gas.

[0048] In some embodiments, the coking oven 1 includes: a carbonization section 101, an activation section 102, and a cooling section 103. The carbonization section 101 has a first furnace chamber and a feed inlet, a first outlet, and a first flue gas outlet connected to the first furnace chamber. The activation section 102 has a second furnace chamber and a second outlet connected to the second furnace chamber and a carbon dioxide inlet for the coking oven. The second furnace chamber is connected to the first furnace chamber through the first outlet. The cooling section 103 has a third furnace chamber and a third outlet connected to the third furnace chamber. The third furnace chamber is connected to the second furnace chamber through the second outlet. The third furnace chamber is equipped with a cooling device.

[0049] In some embodiments, a rich solution pump 8 is connected to the pipeline between the rich solution outlet of the adsorption tower and the rich solution inlet of the first regeneration tower, and a lean solution pump 10 is connected to the pipeline between the lean solution outlet of the regeneration tower and the lean solution inlet of the adsorption tower. The rich solution pump 8 and the lean solution pump 10 provide power for the transport of the rich and lean solutions.

[0050] Another embodiment of this application proposes a zero-carbon emission coking method, utilizing the aforementioned zero-carbon emission coking system, comprising the following steps: The flue gas generated during the coking process in the coking oven 1 enters the secondary combustion furnace 2 for combustion, yielding high-temperature flue gas; after cooling and dust removal, the high-temperature flue gas enters the adsorption tower 6 for adsorption to remove carbon dioxide, yielding amine-containing flue gas; the amine-containing flue gas enters the activated coke adsorber 7 to adsorb the organic amines in the flue gas, yielding clean flue gas, which is then discharged into the atmosphere; the rich liquor saturated in the adsorption tower 6 enters the regeneration tower 11 for regeneration; the lean liquor obtained after regeneration enters the adsorption tower 6 for reuse; the carbon dioxide generated during the regeneration process in the regeneration tower 11 is used as an activation gas and enters the activation section 102 of the coking oven 1 to participate in the preparation of activated coke.

[0051] This application uses captured CO2 as an activator in the preparation of activated carbon. The prepared activated carbon has a well-developed and strong microporous structure, exhibiting good adsorption performance for small molecules. The activation reaction rate is controllable, increasing the yield of activated carbon to over 50%, while also improving the utilization rate of captured CO2.

[0052] This application combines a coking system with a carbon capture system to achieve complete capture of CO2 emitted during the coking process, thus achieving zero carbon emissions during the coking process.

[0053] This application adds an activated coke adsorber 7 after the adsorption tower 6 to effectively adsorb the volatile organic amines during the flue gas purification process, preventing the organic amines from being released into the atmosphere after decarbonization, which would cause serious environmental problems, increase volatile organic compounds, and generate toxic and carcinogenic substances such as nitrosamines in the atmosphere, resulting in secondary pollution.

[0054] It should be noted that this application provides a new use for emitted CO2, which can be used entirely for the production of activated coke, or a portion of the CO2 can be used for the production of activated coke, with the remainder used for other applications such as geological storage and industrial processing.

[0055] Furthermore, the flue gas generated during the coking process in the coking oven 1 includes pyrolysis gas, tar, activation gas, etc., which enter the secondary combustion furnace 2 for complete combustion.

[0056] In some embodiments, the adsorption-saturated rich liquid discharged from the adsorption tower 6 enters the regeneration tower 11 after passing through the first heat exchanger 9. The higher-temperature regenerated lean liquid discharged from the regeneration tower 11 exchanges heat with the lower-temperature adsorption-saturated rich liquid in the first heat exchanger 9 before entering the adsorption tower 6.

[0057] In some embodiments, the system further includes a second heat exchanger 3 and a dust collector 4. The rich liquid saturated with adsorption in the regeneration tower 11 is passed into the second heat exchanger 3 for heat exchange and heating, and the resulting lean liquid and carbon dioxide are returned to the regeneration tower 11. The high-temperature flue gas discharged from the secondary combustion furnace 2 is cooled down by heat exchange with the rich liquid saturated with adsorption in the second heat exchanger 3. The cooled flue gas enters the dust collector 4 for dust removal, and then enters the adsorption tower 6 to remove carbon dioxide.

[0058] In some embodiments, the temperature of the activation section 102 of the coke oven 1 is controlled at 900°C to 1100°C.

[0059] In some embodiments, the adsorbent in the activated coke adsorber 7 comes from the activated coke produced by the coking oven 1. After running for a certain period of time, the activated coke that has been saturated in the activated coke adsorber 7 is discharged into the coking oven 1 for coking, thereby realizing the regeneration and recycling of activated coke.

[0060] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0061] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0062] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between them; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0063] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact with the second feature through an intermediate medium. Furthermore, "above," "over," and "on top" of the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0064] In this invention, the term "some embodiments," etc., refers to specific features, structures, materials, or characteristics described in connection with that embodiment, which are included in at least one embodiment of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiments. Furthermore, the specific features, structures, materials, or characteristics described may be combined in a suitable manner in any one or more embodiments. Moreover, those skilled in the art can combine and integrate the different embodiments described in this specification and the features of the different embodiments without contradiction.

[0065] Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of the present invention.

Claims

1. A zero-carbon emission coking system, characterized in that, include: A coking oven, the coking oven having a first flue gas outlet and a coking oven carbon dioxide inlet, the coking oven comprising: The carbonization section has a first furnace cavity and a feed inlet, a first outlet and a first flue gas outlet connected to the first furnace cavity; An activation section, the activation section having a second furnace chamber and a second outlet connected to the second furnace chamber and the carbon dioxide inlet of the coking oven, the second furnace chamber being connected to the first furnace chamber via a first outlet; The cooling section has a third furnace chamber and a third outlet connected to the third furnace chamber. The third furnace chamber is connected to the second furnace chamber through a second outlet. The third furnace chamber is equipped with a cooling device. The secondary combustion furnace has a first flue gas inlet and a second flue gas outlet on its shell side, and a combustion furnace carbon dioxide inlet and a carbon dioxide outlet on its tube side. The first flue gas outlet is connected to the first flue gas inlet, and the carbon dioxide outlet is connected to the carbon dioxide inlet of the coking oven. The flue gas generated by the coking oven during the coking process enters the secondary combustion furnace for combustion to obtain high-temperature flue gas. An adsorption tower having a second flue gas inlet, a third flue gas outlet, a rich liquid outlet, and a lean liquid inlet, wherein the second flue gas outlet is connected to the second flue gas inlet; An activated coke adsorber has a third flue gas inlet and a clean flue gas outlet, wherein the third flue gas inlet is connected to the third flue gas outlet. The regeneration tower has a first regeneration tower rich liquor inlet, a regeneration tower lean liquor outlet, and a carbon dioxide emission port. The first regeneration tower rich liquor inlet is connected to the adsorption tower rich liquor outlet via a first pipeline, and the regeneration tower lean liquor outlet is connected to the adsorption tower lean liquor inlet via a second pipeline. The first pipeline and the second pipeline are connected via a first heat exchanger to exchange heat between the media in the first pipeline and the second pipeline. The carbon dioxide emission port is connected to the combustion furnace carbon dioxide inlet. The second heat exchanger has its tube side connected to the pipeline connecting the second flue gas outlet and the second flue gas inlet. The regeneration tower also has a rich liquid outlet and a rich liquid inlet. The shell side of the second heat exchanger is connected to the rich liquid outlet and the rich liquid inlet of the regeneration tower respectively through pipelines.

2. The zero-carbon emission coking system according to claim 1, characterized in that, It also includes a dust collector, which is connected to the pipeline connecting the second flue gas outlet of the secondary combustion furnace and the second flue gas inlet of the adsorption tower.

3. The zero-carbon emission coking system according to claim 2, characterized in that, The dust collector is located between the second heat exchanger and the adsorption tower.

4. The zero-carbon emission coking system according to claim 2, characterized in that, It also includes an induced draft fan, which is installed on the pipeline connecting the dust collector and the second flue gas inlet of the adsorption tower.

5. The zero-carbon emission coking system according to claim 1, characterized in that, A rich solution pump is connected to the pipeline between the rich solution outlet of the adsorption tower and the rich solution inlet of the first regeneration tower, and a lean solution pump is connected to the pipeline between the lean solution outlet of the regeneration tower and the lean solution inlet of the adsorption tower.

6. A zero-carbon emission coking method, characterized in that, The coking system using any one of claims 1-5 comprises the following steps: The flue gas generated in the coking oven during the coking process enters the secondary combustion furnace for combustion, resulting in high-temperature flue gas; After being cooled and dusted, the high-temperature flue gas enters the adsorption tower for adsorption to remove carbon dioxide, resulting in amine-containing flue gas. The amine-containing flue gas then enters the activated coke adsorber to adsorb the organic amines in the flue gas, resulting in clean flue gas that is discharged into the atmosphere. The rich liquor saturated in the adsorption tower enters the regeneration tower for regeneration. The lean liquor obtained after regeneration enters the adsorption tower for reuse. The carbon dioxide generated during the regeneration process in the regeneration tower is used as an activation gas and enters the activation section of the coking oven to participate in the preparation of activated coke.

7. The zero-carbon emission coking method according to claim 6, characterized in that, The adsorption-saturated rich liquid discharged from the adsorption tower enters the regeneration tower after passing through the first heat exchanger. The regenerated lean liquid discharged from the regeneration tower at a higher temperature exchanges heat with the adsorption-saturated rich liquid at a lower temperature in the first heat exchanger before entering the adsorption tower.

8. The zero-carbon emission coking method according to claim 6, characterized in that, It also includes a second heat exchanger and a dust collector. The adsorption-saturated rich liquid in the regeneration tower is passed into the second heat exchanger for heat exchange and temperature increase, and the resulting lean liquid and carbon dioxide are returned to the regeneration tower. The high-temperature flue gas discharged from the secondary combustion furnace passes through the second heat exchanger to exchange heat with the adsorption-saturated rich liquid and cool down. The cooled flue gas enters the dust collector for dust removal, and then passes into the adsorption tower to remove carbon dioxide.

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