CN108970595B - Method and system for adsorption desulfurization and desorption regeneration of catalyst efficiency-improving active coke flue gas - Google Patents

Method and system for adsorption desulfurization and desorption regeneration of catalyst efficiency-improving active coke flue gas Download PDF

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CN108970595B
CN108970595B CN201810929925.2A CN201810929925A CN108970595B CN 108970595 B CN108970595 B CN 108970595B CN 201810929925 A CN201810929925 A CN 201810929925A CN 108970595 B CN108970595 B CN 108970595B
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active coke
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gas
flue gas
heat exchange
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CN108970595A (en
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马春元
李军
赵希强
王涛
冯太
夏霄
张世珍
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Shandong University
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Abstract

The invention relates to a method and a system for adsorption desulfurization and desorption regeneration of catalyst-enhanced active coke flue gas, belonging to the field of air pollutant treatment and resource utilization2And water vapor, the metal-based catalyst is melted in a high-temperature region analysis section in the analysis regeneration tower, and the metal-based catalyst permeates and supports the regenerated active coke to obtain a regenerated supported active coke adsorbent in a cooling section; and (4) enabling the regenerated load active coke adsorbent to enter a desulfurization adsorption tower for desulfurization of the flue gas. Not only finish SO2The method can efficiently remove the active coke, and can efficiently load the metal catalyst and the regenerated active coke, thereby improving the desulfurization efficiency of the active coke. One part of the heat exchange medium of the desorption regeneration tower is inert gas, so that the safety of the whole device is improved. The heat of the flue gas generated by the incinerator is fully utilized in the analytic process and the desulfurization process, and the heat is recycled.

Description

Method and system for adsorption desulfurization and desorption regeneration of catalyst efficiency-improving active coke flue gas
Technical Field
The invention belongs to the field of air pollutant treatment and resource utilization, and particularly relates to a method and a system for adsorption desulfurization and desorption regeneration of catalyst-enhanced active coke flue gas.
Background
Under the condition that the current domestic environmental protection situation is increasingly severe, the realization of the clean utilization of fuel and the efficient removal of air pollutants become important research directions of environmental protection researchers. SO in air2Mainly generated by burning fossil fuel in coal-fired power plants or in the steel industryThe gaseous pollutants, which are currently aimed at removing SO2Mainly adopts limestone wet desulphurization technology, has the advantages of high desulphurization efficiency, simple process and the like, but also has the defects of high water consumption and formation of a large amount of inferior desulphurization gypsum (CaSO)4∙2H2O) is easy to cause secondary pollution and the like. The technology for preparing active coke by using coal as a raw material to realize dry flue gas desulfurization is widely researched and utilized due to the advantages of high desulfurization efficiency, no water consumption, no generation of secondary pollutants and the like. SO in flue gas2Adsorbing in active coke with developed pore structure, and realizing SO by thermal regeneration in a desorption reduction tower2Enrichment of separated out and regeneration of sulfur-loaded active coke, separated out SO2The gas can be processed in a centralized way or reused, for example, elemental sulfur (or acid (H) can be prepared by carbothermic reduction reaction under a certain atmosphere2SO4) And the regenerated active coke can enter the desulfurizing tower for recycling, thereby improving the system economy. SO may be achieved by some metal catalysis2However, in the existing process, 201210462982.7 a simultaneous desulfurization and denitrification catalyst is disclosed, which uses active carbon, active coke or active carbon fiber as a carrier, adopts an isometric impregnation method to impregnate the carrier in a mixed solution of praseodymium salt and nickel salt or cobalt salt, dries the carrier sufficiently, and then bakes the dried carrier under the protection of inert gas, and the raw material salt loaded on the carrier is generally difficult to realize the efficient loading of the catalyst and the active coke.
Disclosure of Invention
In view of the problems in the prior art, it is a first object of the present invention to provide a method for adsorptive desulfurization and desorption regeneration of catalyst-enhanced active coke flue gas. In the analytical regeneration tower, the characteristics of different temperature interval distribution of the analytical regeneration tower are utilized, so that the low-melting-point metal-based catalyst is melted in the analytical regeneration tower and uniformly distributed on the surface of active coke, the metal-based catalyst in a molten state in a cooling section is influenced by the pressure difference between the inside and the outside of the active coke, permeates into a coal skeleton structure, and is combined with surface functional groups to realize the deep regulation and control of the active coke; the adsorbent with high catalyst and active coke loading efficiency is prepared.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a method for adsorption desulfurization and desorption regeneration of catalyst efficiency-improving active coke flue gas comprises the following specific steps:
1) parsing and loading
The sulfur-carrying active coke and the metal-based catalyst enter a desorption tower, the sulfur-carrying active coke separates out moisture in the active coke at a preheating section of a desorption regeneration tower, and the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; desorbing sulfur dioxide adsorbed in the sulfur-loaded active coke in the desorption section, leaving the desorption section, and removing the sulfur dioxide out of the room after passing through a reheater of the incinerator; carrying residual SO of sulfur active coke in cooling section2The gas is released and led out and enters an analysis section for centralized treatment, and the sulfur-loaded active coke becomes regenerated active coke in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent;
3) adsorption
The flue gas generated by the incinerator passes through a reheater and then enters a desulfurization adsorption tower, the regenerated loaded active coke adsorbent obtained in the step 2) enters the desulfurization adsorption tower to react with the flue gas and water to adsorb SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
The application realizes the simultaneous analysis and load, and completes the SO2The high-efficiency desorption can be realized, the high-efficiency loading of the metal catalyst and the regenerated active coke can be realized to obtain a high-efficiency adsorbent, the metal-based catalyst is melted in a high-temperature region analysis section in an analysis regeneration tower, and the metal-based catalyst is uniformly distributed on the surface of the active coke; the active coke is cooled in the desorption regeneration towerHowever, local negative pressure is formed inside the porous active coke pores, and at the moment, the molten metal-based catalyst is influenced by the pressure difference between the inside and the outside of the active coke, permeates into the coal skeleton structure and is combined with the surface functional groups to realize the depth control of the active coke.
Preferably, the metal-based catalysts in step 2) are Fe-based, Ni-based and Co-based catalysts, the melting point of the metal catalyst being <500 ℃.
Preferably, the diameter of the active coke in the step 1) is 50 μm-9 mm. Further preferably, the diameter of the active coke in the step 1) is 50 μm to 3 mm.
Preferably, the temperature of the preheating section in the step 1) is 105-150 ℃, the temperature of the analysis section is 300-500 ℃, the temperature of the cooling section is 50-90 ℃, the time of the material in the analysis section is 20 min-2 h, and the time of the material in the cooling section is 20 min-1 h.
Further preferably, the time of the material in the analysis section is 40 min-1.5 h, and the time of the material in the cooling section is 30 min-1 hmin.
Preferably, the temperature of the desulfurization adsorption tower is 60-110 ℃, and the contact time of the regenerated loaded active coke adsorbent and the flue gas in the desulfurization adsorption tower is 3-10 s.
Preferably, the contact time of the regenerated loaded active coke adsorbent and the flue gas in the desulfurization adsorption tower is 5-7 s.
The second purpose of the invention is to provide a system for adsorbing, desulfurizing and desorbing the flue gas of the active coke with catalyst efficiency,
the utility model provides a system for catalyst is carried active coke flue gas and is adsorbed desulfurization and analytic regeneration, including analytic regenerator column, the desulfurization adsorption tower, burn burning furnace, the dust remover, the chimney, inert gas generator, analytic regenerator column is preheating section, analytic section, the cooling zone by last to being in proper order down, preheating section, analytic section, the top of cooling zone sets up gaseous eduction gear respectively, the gaseous eduction gear of analytic section is connected to the gaseous eduction gear of cooling zone, the desulfurization adsorption tower is connected to the gaseous eduction gear of preheating section, the high concentration SO of the gaseous eduction gear of analytic section2The outer walls of the preheating section, the desorption section and the cooling section are provided with heat exchange medium pipesThe box, inert gas generator are connected with the heat transfer medium pipe case of preheating section, analytic section respectively, and the flue gas that burns burning furnace gets into the desulfurization adsorption tower behind the heat transfer medium pipe case of analytic section, and the gas-solid mixture of desulfurization adsorption tower gets into the dust remover, and the solid material of dust remover gets into the desorption tower, and the flue gas gets into the chimney.
Preferably, the adding position of the catalyst is a flue gas inlet of the desulfurization adsorption tower, a sulfur-carrying active coke outlet of the bag-type dust collector or an inlet of the desorption regeneration tower.
Preferably, the inert gas generator is firstly connected with an inlet of the cooling section heat exchange medium pipe box, an outlet of the cooling section heat exchange medium pipe box is connected with an inlet of the preheating section heat exchange medium pipe box, and an outlet of the preheating section heat exchange medium pipe box is connected with the inert gas generator.
The inert gas firstly enters the cooling section to absorb heat and then enters the preheating section to release heat to heat the sulfur-carrying active coke and the catalyst.
Preferably, the cooling section heat exchange medium channel is divided into an upper part and a lower part, the heat exchange medium of the upper part heat exchange medium channel is inert gas, and the heat exchange medium of the lower part heat exchange medium channel is air or water.
The heat exchange medium at the lower part of the cooling section can recover the waste heat of the regenerated load active coke.
Preferably, transverse or vertical heat exchange tubes are arranged in the preheating section, the resolving section and the cooling section; and a condenser is arranged on a pipeline connecting the preheating section gas guiding device and the desulfurization adsorption tower.
Preferably, the gas guiding device comprises a conical funnel, a porous reticular plate and a gas guiding pipe, wherein the conical funnel penetrates through the porous reticular plate, and the gas guiding pipe is positioned above the porous reticular plate.
The invention has the beneficial effects that:
1) the invention provides a flue gas adsorption desulfurization and desorption regeneration process for catalyst efficiency-improving active coke. Controlling the temperature distribution in the reactor according to the conditions required by the analysis process of the powdery active coke material, so that the analysis process is efficiently, safely and stably completed in the analysis regeneration tower;
2) according to the condition that negative pressure appears in active coke particles when the temperature of a cooling section in an analytic regeneration tower is reduced, high-efficiency loading of the catalyst is realized by melting a low-melting-point metal-based catalyst at a high-temperature section and permeating negative pressure into pores at a low-temperature section;
3) one part of a heat exchange medium of the analysis regeneration tower is inert gas, the device possibly has unpredicted loss such as gas leakage and the like, and the safety of the whole device is improved because the inert gas has stable property and does not participate in the reaction in the reactor;
4) high concentration SO from the desorption section of the desorption regeneration tower2The gas absorbs part of the heat of the flue gas of the incinerator through a reheater at the lower part of the incinerator, SO that the temperature of the flue gas of the incinerator can be reduced on the one hand because the temperature of the active coke adsorption cannot be too high, and high-concentration SO is heated on the other hand2Temperature of gas, high concentration SO2The gas can be used in sulfur preparation, sulfuric acid preparation and the like after leaving the incinerator.
5) The inert gas generator is used for preparing inert gas and then sending the inert gas to the cooling section of the desorption tower to exchange heat with the adsorbing material discharged from the desorption section, the inert gas is heated, the adsorbing material is cooled, then the inert gas heat exchange medium is sent to the preheating section of the desorption tower to preheat the adsorbing material, the inert gas is recycled after being discharged from the preheating section, and meanwhile the purpose of energy conservation is achieved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the application and, together with the description, serve to explain the application and are not intended to limit the application.
FIG. 1 is a diagram of a system for adsorptive desulfurization and desorption regeneration of catalyst-enhanced active coke flue gas;
FIG. 2 is a schematic diagram of a desorption tower;
wherein:
1. an air guide material homogenizing device; 2. a preheating section; 3. analyzing the section; 4. a cooling section; 5. an inert gas generator; 6. a desorption regeneration tower; 7. an incinerator; 8. a reheater; 9. a desulfurization adsorption tower; 10. a dust remover; 11. a chimney; 12. a condenser; 13. a main induced draft fan; 14. and a secondary induced draft fan.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The invention will be further illustrated by the following examples
Example 1
1) Parsing and loading
Sulfur-carrying active coke with a diameter of 70 mu m and metal-based catalyst FeCl3The active coke enters an analytic regeneration tower, moisture in the active coke is separated out from the sulfur-carrying active coke at 120 ℃ in a preheating section of the analytic regeneration tower, and the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; at the temperature of 350 ℃ in the desorption section, desorbing sulfur dioxide adsorbed in the sulfur-carrying active coke to leave the desorption section, and removing the sulfur dioxide to the outside for recycling after passing through a reheater of the incinerator; carrying residual SO of sulfur-bearing active coke at the temperature of 60 ℃ in a cooling section2The gas is released and led out and enters an analysis section for centralized treatment, and the sulfur-loaded active coke becomes regenerated active coke in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent, wherein the time of the material in the analysis section is 1.5h, and the time of the material in the cooling section is 30 min;
3) adsorption
Flue gas generated by incineratorPassing the regenerated active coke adsorbent through a reheater, then entering a desulfurization adsorption tower, entering the regenerated active coke adsorbent obtained in the step 2) into the desulfurization adsorption tower, controlling the temperature of the desulfurization adsorption tower at 60 ℃, reacting the regenerated active coke adsorbent with flue gas and water, controlling the contact time to be 5s, and adsorbing SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
Example 2
1) Parsing and loading
Sulfur-carrying active coke with diameter of 1mm and metal-based catalyst FeCl3The active coke enters an analytic regeneration tower, moisture in the active coke is separated out from the sulfur-carrying active coke at 120 ℃ in a preheating section of the analytic regeneration tower, and the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; at the temperature of 400 ℃ in the desorption section, desorbing sulfur dioxide adsorbed in the sulfur-carrying active coke to leave the desorption section, and removing the sulfur dioxide out of the room after passing through a reheater of the incinerator; carrying residual SO of sulfur-bearing active coke at the temperature of 70 ℃ in a cooling section2The gas is released and led out and enters an analysis section for centralized treatment, and the sulfur-loaded active coke becomes regenerated active coke in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent, wherein the time of the material in the analysis section is 1.5h, and the time of the material in the cooling section is 30 min;
3) adsorption
Enabling flue gas generated by the incinerator to pass through a reheater and then enter a desulfurization adsorption tower, enabling the regenerated load active coke adsorbent obtained in the step 2) to enter the desulfurization adsorption tower, enabling the temperature of the desulfurization adsorption tower to be 70 ℃, enabling the regenerated load active coke to react with flue gas and water, enabling the contact time to be 5s, and adsorbing SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
Example 3
1) Parsing and loading
Sulfur-carrying active coke with diameter of 3mm and metal-based catalyst FeCl3The active coke enters an analytic regeneration tower, moisture in the active coke is separated out from the sulfur-carrying active coke at 140 ℃ in a preheating section of the analytic regeneration tower, and the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; at the temperature of 450 ℃ in the desorption section, desorbing sulfur dioxide adsorbed in the sulfur-carrying active coke to leave the desorption section, and removing the sulfur dioxide out of the room after passing through a reheater of the incinerator; carrying residual SO of sulfur-bearing active coke at 75 ℃ in a cooling section2The gas is released and led out and enters an analysis section for centralized treatment, and the sulfur-loaded active coke becomes regenerated active coke in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent, wherein the time of the material in the analysis section is 1h, and the time of the material in the cooling section is 45 min;
3) adsorption
Enabling flue gas generated by the incinerator to pass through a reheater and then enter a desulfurization adsorption tower, enabling the regenerated load active coke adsorbent obtained in the step 2) to enter the desulfurization adsorption tower, enabling the temperature of the desulfurization adsorption tower to be 70 ℃, enabling the regenerated load active coke to react with flue gas and water, enabling the contact time to be 5s, and adsorbing SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
Example 4
1) Parsing and loading
Sulfur-loaded active coke with diameter of 6mm and metal-based catalyst FeCl3The active coke enters an analytic regeneration tower, moisture in the active coke is separated out from the sulfur-carrying active coke at 145 ℃ in a preheating section of the analytic regeneration tower, and the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; at 470 ℃ of the desorption section, desorbing sulfur dioxide adsorbed in the sulfur-carrying active coke to leave the desorption section, and removing the sulfur dioxide out of the desorption section after passing through a reheater of the incinerator; carrying residual SO of sulfur-bearing active coke at the temperature of 80 ℃ in a cooling section2The gas is released and led out and enters an analysis section for centralized treatment, and the sulfur-loaded active coke becomes regenerated active coke in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent, wherein the time of the material in the analysis section is 40min, and the time of the material in the cooling section is 1 h;
3) adsorption
Enabling flue gas generated by the incinerator to pass through a reheater and then enter a desulfurization adsorption tower, enabling the regenerated load active coke adsorbent obtained in the step 2) to enter the desulfurization adsorption tower, enabling the temperature of the desulfurization adsorption tower to be 70 ℃, enabling the regenerated load active coke to react with flue gas and water, enabling the contact time to be 5s, and adsorbing SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
The heat exchange tubes of the desorption regeneration tower with the diameter of the active coke being 50 mu m to 3mm are arranged transversely, and the heat exchange tubes of the desorption regeneration tower with the diameter of the active coke being 3mm to 9mm are arranged vertically.
Example 5
1) Parsing and loading
Sulfur-carrying active coke with diameter of 6mm and metal-based catalyst NiCl2The sulfur-bearing active coke enters an analytic regeneration tower, and is separated out of the active coke at 145 ℃ in a preheating section of the analytic regeneration towerWater, the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; at 470 ℃ of the desorption section, desorbing sulfur dioxide adsorbed in the sulfur-carrying active coke to leave the desorption section, and removing the sulfur dioxide out of the desorption section after passing through a reheater of the incinerator; carrying residual SO of sulfur-bearing active coke at the temperature of 80 ℃ in a cooling section2The gas is released and led out and enters an analysis section for centralized treatment, and the sulfur-loaded active coke becomes regenerated active coke in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent, wherein the time of the material in the analysis section is 40min, and the time of the material in the cooling section is 1 h;
3) adsorption
Enabling flue gas generated by the incinerator to pass through a reheater and then enter a desulfurization adsorption tower, enabling the regenerated load active coke adsorbent obtained in the step 2) to enter the desulfurization adsorption tower, enabling the temperature of the desulfurization adsorption tower to be 60 ℃, enabling the regenerated load active coke to react with flue gas and water, enabling the contact time to be 5s, and adsorbing SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
Example 6
The utility model provides an active coke flue gas adsorption desulfurization and analytic regeneration system is carried to effect to catalyst, including analytic regenerator column 6, desulfurization adsorption tower 9, burn burning furnace 7, dust remover 10, chimney 11, inert gas generator 5, analytic regenerator column 6 is preheating section 2 by last to being in proper order down, analytic section 3, cooling zone 4, preheating section 2, analytic section 3, cooling zone 4's top sets up gaseous eduction gear 1 respectively, cooling zone gas eduction gear connects analytic section gas eduction gear, preheating section gas eduction gear connects the desulfurization adsorption tower, analytic section gas eduction gear's high concentration SO2Enters a reheater 8 of an incinerator 7 and then goes out of the way, a preheating section 2 and a resolving section3. The outer wall of the cooling section 4 is provided with a heat exchange medium pipe box, the inert gas generator 5 is respectively connected with the heat exchange medium pipe box of the preheating section 2 and the analysis section 3, the flue gas of the incinerator 7 enters the desulfurization adsorption tower 9 after passing through the heat exchange medium pipe box of the analysis section 3, the gas-solid mixed material of the desulfurization adsorption tower 9 enters the dust remover 10, the solid material of the dust remover 10 enters the analysis regeneration tower 6, and the flue gas enters the chimney 11.
Preferably, the inert gas generator 5 is firstly connected with an inlet of a cooling section heat exchange medium tube box, an outlet of the cooling section heat exchange medium tube box is connected with an inlet of a preheating section heat exchange medium tube box, and an outlet of the preheating section heat exchange medium tube box is connected with the inert gas generator 5.
Preferably, a condenser 12 is arranged on a pipeline connecting the preheating section gas guiding device and the desulfurization adsorption tower.
Preferably, a main induced draft fan 13 is arranged on a connecting pipeline of the dust remover 10 and the chimney 11.
Preferably, a second-level induced draft fan 14 is arranged on a pipeline connecting the incinerator 7 and the desulfurization adsorption tower 9
Preferably, the cooling section heat exchange medium pipe box is divided into an upper part and a lower part, the heat exchange medium of the upper part heat exchange medium pipe box is inert gas, and the heat exchange medium of the lower part heat exchange medium pipe box is air.
Preferably, the gas leading-out device 1 consists of a conical funnel, a porous reticular plate and a gas guide tube, wherein the conical funnel penetrates through the porous reticular plate, and the gas guide tube is positioned above the porous reticular plate.
Desulfurization degree of the desulfurization adsorption tower:
desulfurization rate in desulfurization adsorption column
Unsupported active coke 80％-85％
Example 1 More than 95 percent
Example 2 More than 95 percent
Example 3 More than 95 percent
Example 4 More than 95 percent
Example 5 Over 98 percent
The desorption rate of the desorption regeneration tower is more than 98 percent; high concentration SO derived from the desorption section of the desorption regeneration tower2The concentration of the gas is 35-45%.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims (13)

1. A method for adsorbing, desulfurizing and analyzing and regenerating active coke flue gas by catalyst efficiency improvement is characterized by comprising the following steps: the method comprises the following specific steps:
1) parsing and loading
The sulfur-carrying active coke and the metal-based catalyst enter an analytical tower, the sulfur-carrying active coke separates out moisture in the active coke at a preheating section of an analytical regeneration tower, and the separated water vapor is led out from the preheating section and enters a desulfurization adsorption tower; the sulfur dioxide adsorbed in the active coke loaded with sulfur in the desorption section is desorbed and leaves the desorption section and passes through an incineratorThe reheater(s) is (are) removed outside the boundary; carrying residual SO of sulfur active coke in cooling section2Gas is released and led out and enters an analysis section for centralized treatment, and sulfur-loaded active coke becomes a regenerated loaded active coke adsorbent in a cooling section;
2) load(s)
Melting the metal-based catalyst in a high-temperature region analysis section in an analysis regeneration tower, and in a cooling section, enabling the metal-based catalyst to permeate and load regenerated active coke to obtain a regenerated loaded active coke adsorbent; the metal-based catalyst is ferric chloride, and the temperature of the desorption section is 350-500 ℃;
3) adsorption
The flue gas generated by the incinerator passes through a reheater and then enters a desulfurization adsorption tower, the regenerated loaded active coke adsorbent obtained in the step 2) enters the desulfurization adsorption tower to react with the flue gas and water to adsorb SO in the flue gas2A gas;
4) separation of
Adsorption of SO2The sulfur-carrying loaded active coke of the gas and the clean flue gas enter a bag-type dust collector to realize gas-solid separation, the sulfur-carrying loaded active coke is collected and sent to an analytic regeneration tower to be analyzed and regenerated, and the clean flue gas is emptied through a chimney after being treated by other pollutants.
2. The method of claim 1, wherein: the diameter of the active coke in the step 1) is 50 μm-9 mm.
3. The method of claim 1, wherein: the diameter of the active coke in the step 1) is 50 μm-3 mm.
4. The method of claim 1, wherein: in the step 1), the temperature of the preheating section is 105-150 ℃, the temperature of the cooling section is 50-90 ℃, the time of the material in the analysis section is 20 min-2 h, and the time of the material in the cooling section is 20 min-1 h.
5. The method of claim 1, wherein: in the step 1), the time of the material in the resolving section is 40 min-1.5 h, and the time of the material in the cooling section is 30 min-1 h.
6. The method of claim 1, wherein: the temperature of the desulfurization adsorption tower is 60-110 ℃, and the contact time of the regenerated load active coke and the flue gas in the desulfurization adsorption tower is 3-10 s.
7. The method of claim 1, wherein: the contact time of the regenerated load active coke adsorbent and the flue gas in the desulfurization adsorption tower is 5-7 s.
8. A system for realizing the method for flue gas adsorption desulfurization and desorption regeneration of catalyst-enhanced active coke according to claim 1, which comprises a desorption regeneration tower, a desulfurization adsorption tower, an incinerator, a dust remover, a chimney and an inert gas generator, wherein the desorption regeneration tower comprises a preheating section, a desorption section and a cooling section from top to bottom in sequence, gas leading-out devices are respectively arranged above the preheating section, the desorption section and the cooling section, the cooling section gas leading-out device is connected with the desorption section gas leading-out device, the preheating section gas leading-out device is connected with the desulfurization adsorption tower, and the desorption section gas leading-out device is high in concentration SO2The outer wall of the preheating section, the analysis section and the cooling section is provided with a heat exchange medium pipe box, the inert gas generator is respectively connected with the heat exchange medium pipe box of the preheating section and the analysis section, the flue gas of the incinerator enters the desulfurization adsorption tower after passing through the heat exchange medium pipe box of the analysis section, the gas-solid mixed material of the desulfurization adsorption tower enters the dust remover, the solid material of the dust remover enters the analysis tower, and the flue gas enters the chimney.
9. The system of claim 8, wherein: the adding position of the catalyst is a flue gas inlet of the desulfurization adsorption tower, a sulfur-carrying active coke outlet of the bag-type dust remover or an inlet of the desorption regeneration tower.
10. The system of claim 8, wherein: the inert gas generator is connected with an inlet of the cooling section heat exchange medium pipe box, an outlet of the cooling section heat exchange medium pipe box is connected with an inlet of the preheating section heat exchange medium pipe box, and an outlet of the preheating section heat exchange medium pipe box is connected with the inert gas generator.
11. The system of claim 8, wherein: the cooling section heat exchange medium pipe box is divided into an upper part and a lower part, the heat exchange medium of the upper part heat exchange medium pipe box is inert gas, and the heat exchange medium of the lower part heat exchange medium pipe box is air.
12. The system of claim 8, wherein: transverse or vertical heat exchange tubes are arranged in the preheating section, the resolving section and the cooling section; and a condenser is arranged on a pipeline connecting the preheating section gas guiding device and the desulfurization adsorption tower.
13. The system of claim 8, wherein: the gas guiding device is composed of a conical funnel, a porous reticular plate and a gas guide tube, wherein the conical funnel penetrates through the porous reticular plate, and the gas guide tube is positioned above the porous reticular plate.
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