WO2019134270A1 - 一种焦炉烟气净化中吸附剂的再生系统及再生方法 - Google Patents

一种焦炉烟气净化中吸附剂的再生系统及再生方法 Download PDF

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WO2019134270A1
WO2019134270A1 PCT/CN2018/081030 CN2018081030W WO2019134270A1 WO 2019134270 A1 WO2019134270 A1 WO 2019134270A1 CN 2018081030 W CN2018081030 W CN 2018081030W WO 2019134270 A1 WO2019134270 A1 WO 2019134270A1
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adsorbent
gas
coke oven
analytical
regenerated
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PCT/CN2018/081030
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English (en)
French (fr)
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朱廷钰
李玉然
张帅
王斌
林玉婷
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中国科学院过程工程研究所
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Publication of WO2019134270A1 publication Critical patent/WO2019134270A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
    • B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40086—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by using a purge gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas

Definitions

  • the invention belongs to the technical field of flue gas purification equipment, relates to a regeneration system and a regeneration method of an adsorbent in a coke oven flue gas purification, in particular to a regeneration system and regeneration of an adsorbent in a coke oven flue gas purification for simultaneously recovering by-products. method.
  • activated carbon As a porous material with large specific surface area, developed pore structure and rich functional groups, activated carbon has been applied to many aspects such as flue gas purification and water treatment. Flue gas purification with activated carbon in the steel industry application technology is more mature, this technique not only simultaneous removal of SO 2 in the flue gas and NO x, but also has no water, no secondary pollution, effective removal of dust and fumes Contaminants such as heavy metals (such as mercury) can be recycled to recover sulfur resources through adsorbents, which can be well applied to the purification of flue gas in coal-fired power plants, sintering machines, coke ovens and waste incineration. Compared with other treatment methods such as wet desulfurization and SCR denitration, the most significant advantage of the activated carbon process is that no by-products or three waste materials are produced in the process.
  • the activated carbon method flue gas purification process can obtain a higher denitration rate, and at the same time adsorb and remove the H 2 S, HCN, tar and volatile organic compounds in the coke oven flue gas. Harmful Substance. After the adsorption of activated carbon is saturated, it needs to be regenerated to recycle and reduce the purification cost.
  • the composition of the analytical gas generated by the regeneration process is complex, mainly N 2 , SO 2 , CO, CO 2 , CH 4 and volatile organic substances, etc., generally absorbed by ammonia water.
  • the SO 2 preparation of ammonium sulfate, and the coking plant itself has a ammonium sulfate section, which can be well combined with the regeneration process to reduce the investment operating costs.
  • the invention patent CN 103861439A discloses a flue gas desulfurization and denitration process combined with ammonia desulfurization and activated carbon denitration.
  • the ammonia desulfurization is a relatively mature wet desulfurization process
  • the activated carbon denitration is a dry denitration process
  • the activated carbon is in the process.
  • the process is recycled, that is, the adsorption is saturated and then analyzed in the regeneration tower to simultaneously desulfurize, denitrify, remove dust, remove mercury and volatile organic compounds.
  • this patent does not address how to process by-products produced during the process.
  • the invention patent CN 106693603A discloses an activated carbon method flue gas purification device and a purification treatment method.
  • the device comprises an activated carbon absorption tower and an activated carbon analysis tower.
  • the treatment process is divided into two steps of activated carbon adsorption purification and analytical regeneration, and the absorption tower is introduced in detail.
  • the internal structure briefly describes the process flow, and does not explain the use, loss and disposal of the materials involved in the system. It does not discuss the recycling of waste residue and waste gas.
  • the present invention provides a regeneration system and a regeneration method of the adsorbent in the coke oven flue gas purification.
  • the invention develops and designs a flue gas purification process suitable for a coke oven by optimizing the flue gas purification and regeneration process of the coke oven and combining the resource advantages of the coke oven and the coking plant. While exerting the function of removing activated carbon, it does not produce any by-products that are difficult to use, and truly clean and efficient flue gas purification.
  • the present invention provides a regeneration system for an adsorbent in a coke oven flue gas purification, the system comprising an analytical tower, a screening device, a purification device, a sulfur ammonium treatment section, and a coke oven;
  • the top of the analytical tower is provided with a feed inlet for the adsorbent to be regenerated, and the bottom is provided with a regenerating adsorbent discharge port, the regenerative adsorbent discharge port is connected to the screening device, and the analytical tower includes heating at the upper portion.
  • a cooling section located below the heating section, the heat source inlet of the heating section is connected to the heat source generating device, the heat source outlet of the heating section is returned to the heat source generating device, the cold source inlet of the cooling section is connected to the cold source; and the lower part of the analytical tower is provided with a blowing
  • the scavenging inlet has an analytical gas outlet connected to the upper portion, and the analytical gas outlet is connected to the ammonium sulfate treatment section and the coke oven.
  • the regeneration process mainly includes the regeneration of the adsorbent and the post-treatment of the analytical gas.
  • the activated carbon is analyzed at a high temperature, and the coke oven gas is heated by the hot air furnace to supply heat.
  • the analytical gas containing SO 2 is discharged from the analytical tower and then passed through the dust removal and purification.
  • the plant's ammonium sulfate section recovers the sulfur resources, and the remaining CO-containing gas enters the coke oven combustion chamber to participate in the combustion, so that waste residue and waste gas are generated during the regeneration process.
  • the analytical column is an adsorbent regeneration reactor, and the analytical gas obtained from the analytical column mainly contains N 2 , SO 2 and CO, and after passing through the sulfuric acid section of the coking plant to recover sulfur resources therein, it mainly contains N 2 .
  • CO wherein the CO concentration can reach about 20%, can be used as fuel into the main pipeline of the coke oven gas, and finally enters the coke oven combustion chamber to participate in combustion.
  • the ammonium sulfate treatment section is an existing ammonium sulfate treatment section in a coking plant and is prior art.
  • the regeneration system and regeneration method of the adsorbent in the coke oven flue gas purification relates to coke oven gas, nitrogen gas, coking wastewater treatment and coke oven in the coking plant.
  • Coke oven gas is used as the heating medium of the heat source generating device; nitrogen is used as the purging gas of the regeneration tower to obtain the analytical gas of concentrated SO 2 ; the activated carbon powder under the sieve is used as the water treatment adsorbent in the sewage treatment section; the analytical gas can enter the ammonium sulfate
  • the recovery section recovers sulfur resources and enters the coke oven combustion chamber as a fuel to recover combustible components.
  • the sieving device sifts the sieved material and the undersize material, and the sieve top material is subjected to adsorption-analysis recycling for the regenerated adsorbent, and the sieve material participates in the coking wastewater treatment and / or coal blending coke.
  • the undersize material can be sent to participate in the coking wastewater treatment process, and after the adsorption capacity is significantly reduced, it is sent to the coal blending workshop to participate in coal blending coking.
  • the undersize material comprises a slag having a particle size of > 2 mm and a powder having a particle size of ⁇ 2 mm, wherein the slag may have a particle size of 3 mm, 4 mm, 5 mm, 6 mm, 7 mm or 8 mm, etc., and larger particles.
  • the diameter is not limited to the numerical values listed, and other numerical values not included in the numerical range are also applicable; the particle size of the powder may be 1.7 mm, 1.5 mm, 1.3 mm, 1 mm, 0.7 mm, 0.5 mm or 0.3 mm.
  • Etc. and smaller particle sizes but are not limited to the numerical values listed, and other unexemplified values within the numerical range are equally applicable.
  • the undersize material includes activated carbon slag having a particle size of > 2 mm and activated carbon powder having a particle size of less than 2 mm.
  • the slag having a particle size of >2 mm is sent to a coking wastewater treatment process for use as a water treatment adsorbent, and the powder having a particle size of ⁇ 2 mm participates in coal blending coking.
  • the screening device is a vibrating screen.
  • a discharge valve is provided between the regenerating adsorbent discharge port and the screening device for controlling the rate of movement of the adsorbent in the analytical column.
  • the heat source generating device is a hot air furnace, which generates flue gas having a temperature of 450 ° C to 550 ° C as a heat source of the analytical tower; wherein the temperature of the flue gas can be 450 ° C, 460 ° C, 470 °C, 480°C, 490°C, 500°C, 510°C, 520°C, 530°C, 540°C or 550°C, etc., but are not limited to the numerical values listed, and other numerical values not included in the numerical range are equally applicable.
  • a gas delivery device is disposed between the heat source inlet of the heating section and the heat source generating device.
  • the gas delivery device is a circulation fan.
  • the heating medium of the hot blast stove is gas.
  • the gas is a combination of any one or at least two of coke oven gas, coke oven blast furnace mixed gas, blast furnace gas or natural gas, and typical but non-limiting examples of the combination are: coke oven gas and coke oven blast furnace
  • coke oven gas and coke oven blast furnace The combination of mixed gas, the combination of blast furnace gas and natural gas, the combination of coke oven gas, coke oven blast furnace mixed gas and blast furnace gas, the combination of coke oven blast furnace mixed gas, blast furnace gas and natural gas.
  • the natural gas may be purchased natural gas, and the general coking plant has sufficient gas, and the amount of the process is not large enough to meet the demand.
  • the source of cold is air.
  • the cold source is generated by a fan connected to a cold source inlet of the cooling section.
  • the purge gas inlet is located below the cooling section in the analytical column.
  • the purge gas is nitrogen, which may be derived from nitrogen produced in a plant space division process or separately purchased by a nitrogen generator to produce nitrogen.
  • the amount of nitrogen used is relatively small, and a nitrogen generator can also be purchased for the process system.
  • the purge gas inlet is connected to a nitrogen generating device.
  • the analytical gas outlet is located above the heating section in the analytical column.
  • a purification device is disposed between the analytical gas outlet and the ammonium sulfate treatment section, and the purification device mainly removes dust in the analytical gas.
  • the purification device is a bag dust removal device.
  • the adsorbent to be regenerated is a desulfurization adsorbent.
  • the desulfurization adsorbent is activated carbon and/or activated coke, preferably activated carbon.
  • the shape of the adsorbent to be regenerated is any one or a combination of at least two of particles, cylinders, spheres or flakes, and a typical but non-limiting example of the combination is: a combination of particles and cylinders , a combination of spheres and flakes, a combination of particles, cylinders and spheres, a combination of particles, cylinders, spheres and flakes, and the like.
  • the adsorbent to be regenerated is from an adsorbent used in coke oven coke oven flue gas purification.
  • the present invention provides a method for regenerating an adsorbent in coke oven flue gas purification, the method comprising the steps of:
  • the adsorbent to be regenerated according to step (a) is a desulfurization adsorbent.
  • the desulfurization adsorbent is activated carbon and/or activated coke, preferably activated carbon.
  • the shape of the adsorbent to be regenerated in step (a) is any one or a combination of at least two of particles, cylinders, spheres or flakes, and typical but non-limiting examples of the combinations are: The combination of cylinders, the combination of spheres and flakes, the combination of particles, cylinders and spheres, the combination of particles, cylinders, spheres and flakes.
  • the adsorbent to be regenerated according to step (a) is derived from the adsorbent used in the coke oven coke oven flue gas purification.
  • the temperature of the heating analysis in the step (a) is 450 ° C to 550 ° C, for example, 450 ° C, 460 ° C, 470 ° C, 480 ° C, 490 ° C, 500 ° C, 510 ° C, 520 ° C, 530 ° C, 540 ° C Or 550 ° C, etc., but is not limited to the numerical values listed, and other numerical values not included in the numerical range are also applicable.
  • the screening in step (b) is carried out in a screening device.
  • the undersize of step (b) comprises a slag having a particle size of > 2 mm and a powder having a particle size of ⁇ 2 mm.
  • the particle size of the powder may be 1.7 mm, 1.5 mm, 1.3 mm, 1 mm, 0.7 mm, 0.5 mm or 0.3 mm, etc., and a smaller particle size, but is not limited to the numerical values listed, and other values within the numerical range The same values are not listed.
  • the undersize material includes activated carbon slag having a particle size of > 2 mm and activated carbon powder having a particle size of less than 2 mm.
  • the slag having a particle size of >2 mm is sent to a coking wastewater treatment process for use as a water treatment adsorbent, and the powder having a particle size of ⁇ 2 mm participates in coal blending coking.
  • the purge gas of step (c) is nitrogen.
  • the analytical gas of step (c) comprises N 2 , SO 2 and CO;
  • the volume content of SO 2 in the analytical gas is controlled to be 5% to 20% by controlling the amount of purge gas supplied, for example, 5%, 8%, 10%, 12%, 15%, 18 % or 20%, etc., but is not limited to the numerical values listed, and other numerical values not included in the numerical range are also applicable, preferably 10% to 15%.
  • the analytical gas is passed into the ammonium sulfate treatment section to recover sulfur after the volume content of CO is 10% to 25%, for example, 10%, 13%, 15%, 17%, 20%, 23% or 25%, etc., but not limited to the numerical values listed, and other unexemplified numerical values within the numerical range are equally applicable.
  • step (c) the analytical gas is subjected to a purification treatment and then passed to a ammonium sulfate treatment section to recover sulfur.
  • the method includes the following steps:
  • the analytical gas is obtained by purging nitrogen gas into the analytical column, and the volume of SO 2 in the analytical gas is controlled to be 5% to 20% by controlling the amount of purge gas supplied. After purification treatment, it is passed into the ammonium sulfate treatment section to recover sulfur, and then enters the coke oven as fuel for combustion.
  • the present invention has the following beneficial effects:
  • Regeneration system and method for regenerating a coke oven gas purification adsorbent the main flue of Coke Oven adsorbent for use in the process, the flue gas is adsorbed by the adsorbent to remove SO 2, NO x, Heavy metals, dust, H 2 S and volatile organic compounds and other harmful substances enter the analytical tower for regeneration, no waste is generated during the regeneration process, and by-product adsorbent powder (slag) is applied to sewage purification and coke oven coking, and analytical gas recovery
  • the sulfur after coke oven participates in the combustion;
  • the regeneration system and the regeneration method of the invention solve the problem of recycling of by-products, and the activated carbon adsorption purification process can truly realize the efficient and clean flue gas purification.
  • FIG. 1 is a schematic structural view of a regeneration system of an adsorbent in a coke oven flue gas purification according to the present invention
  • FIG. 2 is a schematic structural view of a regeneration system of an adsorbent in a coke oven flue gas purification according to Embodiment 1 of the present invention
  • FIG. 3 is a schematic structural view of a regeneration system of an adsorbent in a coke oven flue gas purification according to Embodiment 2 of the present invention
  • 1-analysis tower 2-screening device, 3-heat source generator, 4-sulfur ammonium treatment section, 5-coke furnace, 6-fan, 7-purification device, 8-adsorption tower bucket lifter, 9- Adsorbent buffer tank.
  • a specific embodiment of the present invention provides a regeneration system and a regeneration method for an adsorbent in a coke oven flue gas purification.
  • the system includes an analytical tower 1, a screening device 2, a heat source generating device 3, and sulfur. Ammonium treatment section 4 and coke oven 5;
  • the top of the analytical tower 1 is provided with a feed inlet for the adsorbent to be regenerated, and the bottom is provided with a regenerating adsorbent discharge port, and the regenerated adsorbent discharge port is connected to the screening device 2, wherein the analytical tower 1 is located An upper heating section and a cooling section located below the heating section, the heat source inlet of the heating section is connected to the heat source generating device 3, the heat source outlet of the heating section is returned to the heat source generating device 3, and the cold source inlet of the cooling section is connected to the cold source;
  • the lower portion of the tower 1 is provided with a purge gas inlet, the upper portion is provided with an analytical gas outlet, and the analytical gas outlet is connected to the ammonium sulfate treatment section 4 and the coke oven 5.
  • the method includes the following steps:
  • the purge gas is supplied to the analysis column 1 to be purged, and the analysis gas is obtained.
  • the analysis gas is passed through the ammonium sulfate treatment section 4 to recover sulfur, and then enters the coke oven 5 to be burned as fuel.
  • the embodiment provides a regeneration system and a regeneration method of the adsorbent in the coke oven flue gas purification.
  • the system includes an analytical tower 1, a screening device 2, a heat source generating device 3, and a sulfur ammonium treatment section. 4 and coke oven 5 and fan 6;
  • the top of the analytical tower 1 is provided with a feed inlet for the adsorbent to be regenerated, and the bottom is provided with a regenerating adsorbent discharge port, the recirculating adsorbent discharge port is connected with the screening device 2, and the reclaimed adsorbent discharge port and the sieve are regenerated.
  • a discharge valve is disposed between the sub-devices 2, and the analysis tower 1 includes a heating section located at an upper portion and a cooling section located below the heating section, the heat source inlet of the heating section is connected to the heat source generating device 3, and the heat source inlet of the heating section is A circulation fan is disposed between the heat source generating devices 3, and the heat source outlet of the heating section is returned to the heat source generating device 3, the cold source inlet of the cooling section is connected to the cold source, the cold source is generated by the fan 6, and the lower portion of the analytical tower 1 is provided with a purge gas inlet.
  • the upper part is provided with a resolution gas outlet, the analytical gas outlet is connected with the ammonium sulfate treatment section 4 and the coke oven 5; the heating medium of the hot air furnace is coke oven gas, and the adsorbent is the granular activated carbon used in the coke oven flue gas purification of the coking plant
  • the screening device 2 is a vibrating screen.
  • the processing method of the system includes the following steps:
  • the undersize material comprises a slag having a particle size of >2 mm and a powder having a particle size of ⁇ 2 mm, and the slag having a particle size of >2 mm is sent to the coking wastewater treatment process as a water treatment adsorbent, and the purification capacity is significantly reduced.
  • the coal blending workshop participates in coal blending coking, and the wastewater treatment section can not directly go to coal blending coking, and the powder with a particle size of ⁇ 2 mm participates in coal blending coking;
  • the analytical gas is supplied to the analytical column 1 by purging nitrogen gas, and the amount of SO 2 in the analytical gas is controlled to 15% by controlling the amount of purge gas to be supplied, and the gas is introduced into the analytical gas.
  • the sulfur is recovered in the ammonium sulfate treatment section 4, and the volume of CO in the gas after the recovery of sulfur reaches 20%, and it enters the coke oven 5 to be burned as a fuel.
  • the system and method described in this embodiment does not generate any waste and solves the problem of recycling of by-products.
  • the embodiment provides a regeneration system and a regeneration method of the adsorbent in the coke oven flue gas purification.
  • the structure of the system refers to the structure in Embodiment 1, except that, as shown in FIG. 3, the system further includes purification.
  • the device 7 is located between the analytical gas outlet and the ammonium sulfate treatment section 4, the purification device 7 is a bag dust removal device; and the heating medium of the hot air furnace is a coke oven blast furnace mixed gas.
  • the regeneration method refers to the method in Embodiment 1, except that the adsorbent is the cylindrical activated coke to be regenerated from the coke oven coke oven flue gas purification; the analytical temperature in the step (a) is 460 ° C; In step (b), the slag having a particle size of >2 mm is sent to the coking wastewater treatment plant, and then concentrated and sold to the activated carbon recovery manufacturer for recycling or small furnace kiln for fuel; in step (c), nitrogen is supplied to the analytical column 1 for purging.
  • the adsorbent is the cylindrical activated coke to be regenerated from the coke oven coke oven flue gas purification
  • the analytical temperature in the step (a) is 460 ° C
  • the slag having a particle size of >2 mm is sent to the coking wastewater treatment plant, and then concentrated and sold to the activated carbon recovery manufacturer for recycling or small furnace kiln for fuel
  • step (c) nitrogen is supplied to the analytical column 1 for purging.
  • the analytical gas is removed by the purification device 7 and then passed to the ammonium sulfate treatment section 4 to recover sulfur, and then enter The coke oven 5 is burned as a fuel.
  • the system and method described in this embodiment does not generate any waste and solves the problem of recycling of by-products.
  • the embodiment provides a regeneration system and a regeneration method of the adsorbent in the coke oven flue gas purification.
  • the structure of the system refers to the structure in the first embodiment, except that the heating medium of the hot air furnace is blast furnace gas.
  • the regeneration method refers to the method in Embodiment 1, except that the adsorbent is the spherical activated carbon to be regenerated used in the coke oven flue gas purification; the analytical temperature in the step (a) is 540 ° C; c) The middle of the analytical column 1 is purged with nitrogen to obtain a solution gas, and the volume of SO 2 in the analytical gas is controlled to 20% by controlling the amount of purge gas, and the analytical gas is removed by the purification device 7 After the dust is passed into the ammonium sulfate treatment section 4, sulfur is recovered, and then enters the coke oven 5 to be burned as a fuel.
  • the adsorbent is the spherical activated carbon to be regenerated used in the coke oven flue gas purification
  • the analytical temperature in the step (a) is 540 ° C
  • c) The middle of the analytical column 1 is purged with nitrogen to obtain a solution gas, and the volume of SO 2 in the analytical gas is controlled to 20% by controlling
  • the system and method described in this embodiment does not generate any waste and solves the problem of recycling of by-products.
  • the regeneration system and the regeneration method of the adsorbent in the coke oven flue gas purification according to the present invention fully combine the resource advantages of the coking plant plant area, and on the premise of ensuring the flue gas purification and removal effect,
  • the waste generated in the system is recycled and reused, that is, no waste is generated and resources are saved.
  • the efficient purification of coke oven flue gas is realized, and new process technology support or old process for coking plant flue gas purification is provided. Transforming the reference is of great significance.
  • the present invention illustrates the detailed process equipment and process flow of the present invention by the above embodiments, but the present invention is not limited to the above detailed process equipment and process flow, that is, does not mean that the present invention must rely on the above detailed process equipment and The process can only be implemented. It should be apparent to those skilled in the art that any modifications of the present invention, equivalent substitution of the various materials of the products of the present invention, addition of auxiliary components, selection of specific means, and the like, are all within the scope of the present invention.

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  • Separation Of Gases By Adsorption (AREA)

Abstract

一种焦炉烟气净化吸附剂的再生系统及再生方法。再生系统包括解析塔（1）、筛分装置（2）、净化装置（7）、硫铵处理段（4）和焦炉（5）；解析塔（1）的再生吸附剂出料口与筛分装置（2）相连，解析塔（1）内有加热段和冷却段，加热段的热源入口连接热源发生装置（3），加热段的热源出口返回热源发生装置（3），冷却段的冷源入口连接冷源；解析塔（1）的解析气出口连接硫铵处理段（4）和焦炉（5）。吸附剂在解析塔（1）内被解析，经吹扫形成的SO 2浓缩气，经硫铵处理段（4）脱硫后，剩余的气体通入焦炉燃烧室作为燃料。解析后的吸附剂经筛分后再次参与烟气净化，筛下的粉渣用于水处理和配煤炼焦，完全不产生难处理三废及有害物质，实现了清洁高效的焦炉烟气治理。

Description

一种焦炉烟气净化中吸附剂的再生系统及再生方法 技术领域
本发明属于烟气净化设备技术领域，涉及一种焦炉烟气净化中吸附剂的再生系统及再生方法，尤其涉及一种同时回收副产物的焦炉烟气净化中吸附剂的再生系统及再生方法。
背景技术
活性炭作为一种比表面积大、孔隙结构发达、官能团丰富的多孔性物质，已经应用于烟气净化和水处理等多个方面。活性炭法烟气净化技术在钢铁行业应用较为成熟，该技术不仅能够同时脱除烟气中的SO 2和NO x，还具有不耗水、无二次污染、有效脱除烟气中的粉尘和重金属(如汞)等污染物、可通过吸附剂再生回收硫资源等优点，可以很好的应用于燃煤电厂、烧结机、焦炉和垃圾焚烧等领域的烟气净化治理。相比于其他的处理方法如湿法脱硫与SCR脱硝的组合工艺，活性炭法最显著的优点还在于过程中不产生难以利用的副产物或三废物质。
由于焦炉烟气的低硫高氮的特性，活性炭法烟气净化工艺可以获得较高的脱硝率，同时可吸附脱除焦炉烟气中的H 2S、HCN、焦油以及挥发性有机物等有害物质。活性炭吸附饱和后需要进行再生以循环利用降低净化成本，再生过程产生的解析气中成分复杂，主要为N 2、SO 2、CO、CO 2、CH 4和易挥发有机物等，一般使用氨水吸收其中的SO 2制备硫铵，而焦化厂本身具有硫铵工段，可以很好的和再生工艺相结合，降低投资运行成本。
发明专利CN 103861439A中公开了一种氨法脱硫和活性炭法脱硝联合的烟气脱硫脱硝工艺，氨法脱硫为现有的较为成熟的湿法脱硫工艺，活性炭法脱硝 为干法脱硝工艺，活性炭在工艺中循环利用，即吸附饱和后进再生塔解析，起到同时脱硫、脱硝、除尘、除汞和挥发性有机物的作用。但该专利并未涉及到如何处理过程中所产生的副产物。
发明专利CN 106693603A公开了一种活性炭法烟气净化装置及净化处理方法，装置包括活性炭吸收塔和活性炭解析塔，处理过程分为活性炭吸附净化和解析再生两步，其详细的介绍了吸收塔的内部结构，简单的叙述了工艺的流程，对系统所涉及的物料的使用、损耗和废弃等情况没有作任何说明，没有论述对废渣和废气的回收利用。
因此，针对活性炭法烟气净化工艺设计系统的后处理方法进行研究，保证活性炭再生工艺的顺利实施，进而确保活性炭法烟气净化工艺不产生废渣和废气，实现高效清洁利用，具有非常重要的意义。
发明内容
针对现有烟气净化工艺中无法有效处理废气和废渣的问题，本发明提供了一种焦炉烟气净化中吸附剂的再生系统及再生方法。本发明通过对焦炉烟气净化再生工艺的优化，结合焦炉和焦化厂厂区资源优势，开发设计了适合于焦炉的烟气净化工艺。在发挥活性炭脱除作用的同时，不产生任何难以利用的副产物，真正实现的清洁高效的烟气净化。
为达此目的，本发明采用以下技术方案：
第一方面，本发明提供了一种焦炉烟气净化中吸附剂的再生系统，所述系统包括解析塔、筛分装置、净化装置、硫铵处理段和焦炉；
其中，所述解析塔顶部设有待再生吸附剂进料口，底部设有再生吸附剂出料口，所述再生吸附剂出料口与筛分装置相连，所述解析塔内包括位于上部的加热段和位于加热段下方的冷却段，所述加热段的热源入口连接热源发生装 置，加热段的热源出口返回热源发生装置，冷却段的冷源入口连接冷源；所述解析塔下部设有吹扫气入口，上部设有解析气出口，所述解析气出口连接硫铵处理段和焦炉。
在进行焦炉烟气净化时，所用吸附剂如活性炭和/或活性焦达到饱和后，通过再生工艺完成解析进而进行循环利用。再生工艺主要包括吸附剂再生以及解析气的后处理，活性炭在高温加热时进行解析，通过热风炉燃烧焦炉煤气供热，含有SO 2的解析气从解析塔排出后经除尘净化后通入焦化厂硫铵工段回收其中的硫资源，剩余的含CO气体再进入焦炉燃烧室参与燃烧，以使再生过程中产生废渣和废气。
本发明中，解析塔为吸附剂再生反应器，从解析塔得到的解析气中主要含有N 2、SO 2和CO，通入焦化厂硫铵工段回收其中的硫资源后，其主要含有N 2和CO，其中CO浓度可达到20％左右，可作为燃料通入到焦炉煤气主管道中，最终进入焦炉燃烧室参与燃烧。
本发明中，所述硫铵处理段为焦化厂中现有的硫铵处理段，为现有技术。
本发明所述的焦炉烟气净化中吸附剂的再生系统及再生方法涉及到焦化厂的焦炉煤气、氮气、焦化废水处理和焦炉等。焦炉煤气作为热源发生装置的供热介质；氮气作为再生塔的吹扫气，得到浓缩SO 2的解析气；筛下活性炭粉去污水处理工段作为水处理吸附剂使用；解析气可以进硫铵回收工段回收硫资源，同时进入焦炉燃烧室作为燃料回收利用可燃组分。
以下作为本发明优选的技术方案，但不作为本发明提供的技术方案的限制，通过以下技术方案，可以更好地达到和实现本发明的技术目的和有益效果。
作为本发明优选的技术方案，所述筛分装置筛分得到筛上物和筛下物，所 述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物参与焦化废水处理和/或配煤炼焦。
其中，所述筛下物可以先送去参与焦化废水处理工序，待其吸附能力明显下降后，送去配煤车间参与配煤炼焦。
优选地，所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物去，其中渣状物的粒度可为3mm、4mm、5mm、6mm、7mm或8mm等以及更大粒径，但并不仅限于所列举的数值，该数值范围内其他未列举的数值同样适用；粉状物的粒径可为1.7mm、1.5mm、1.3mm、1mm、0.7mm、0.5mm或0.3mm等以及更小粒径，但并不仅限于所列举的数值，该数值范围内其他未列举的数值同样适用。例如，筛下物包括粒度＞2mm的活性炭渣和粒度小于2mm的活性碳粉。
优选地，所述粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，所述粒度＜2mm的粉状物参与配煤炼焦。
优选地，所述筛分装置为震动筛。
优选地，所述再生吸附剂出料口与筛分装置之间设置卸料阀，其用于控制吸附剂在解析塔中的移动速率。
作为本发明优选的技术方案，所述热源发生装置为热风炉，其产生温度为450℃～550℃的烟气作为解析塔的热源；其中，烟气的温度可为450℃、460℃、470℃、480℃、490℃、500℃、510℃、520℃、530℃、540℃或550℃等，但并不仅限于所列举的数值，该数值范围内其他未列举的数值同样适用。
优选地，所述加热段的热源入口与热源发生装置之间设置气体输送装置。
优选地，所述气体输送装置为循环风机。
优选地，所述热风炉的供热介质为煤气。
优选地，所述煤气为焦炉煤气、焦炉高炉混合煤气、高炉煤气或天然气中任意一种或至少两种的组合，所述组合典型但非限制性实例有：焦炉煤气和焦炉高炉混合煤气的组合，高炉煤气和天然气的组合，焦炉煤气、焦炉高炉混合煤气和高炉煤气的组合，焦炉高炉混合煤气、高炉煤气和天然气的组合等。其中，所述天然气可为外购天然气，一般焦化厂煤气充足，且本工艺用量不大，可以满足需求。
优选地，所述冷源为空气。
优选地，所述冷源由风机产生，风机与冷却段的冷源入口相连。
作为本发明优选的技术方案，所述吹扫气入口位于解析塔中冷却段下方。
优选地，所述吹扫气为氮气，所述氮气可来自于厂区空分工序制得的氮气或另外购置制氮机产生氮气。本发明中，氮气的用量相对较小，也可以购置制氮机给该工艺系统专用。
优选地，所述吹扫气入口连接氮气产生装置。
优选地，所述解析气出口位于解析塔中加热段上方。
作为本发明优选的技术方案，所述解析气出口与硫铵处理段之间设置净化装置，所述净化装置主要脱除解析气中的粉尘。
优选地，所述净化装置为布袋除尘装置。
作为本发明优选的技术方案，所述待再生吸附剂为脱硫吸附剂。
优选地，所述脱硫吸附剂为活性炭和/或活性焦，优选为活性炭。
优选地，所述待再生吸附剂的形状为颗粒、圆柱体、球体或片状体中任意一种或至少两种的组合，所述组合典型但非限制性实例有：颗粒和圆柱体的组合，球体和片状体的组合，颗粒、圆柱体和球体的组合，颗粒、圆柱体、球体和片状体的组合等。
优选地，所述待再生吸附剂来自焦化厂焦炉烟气净化中所用的吸附剂。
第二方面，本发明提供了一种焦炉烟气净化中吸附剂的再生方法，所述方法包括以下步骤：
(a)将待再生吸附剂在解析塔中进行加热解析并冷却，得到再生物料；
(b)将再生物料进行筛分得到筛上物和筛下物，所述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物参与焦化废水处理和/或配煤炼焦；
(c)解析完成后，向解析塔中通入吹扫气进行吹扫后得到解析气，解析气通入硫铵处理段回收硫，然后进入焦炉作为燃料燃烧。
作为本发明优选的技术方案，步骤(a)所述待再生吸附剂为脱硫吸附剂。
优选地，所述脱硫吸附剂为活性炭和/或活性焦，优选为活性炭。
优选地，步骤(a)所述待再生吸附剂的形状为颗粒、圆柱体、球体或片状体中任意一种或至少两种的组合，所述组合典型但非限制性实例有：颗粒和圆柱体的组合，球体和片状体的组合，颗粒、圆柱体和球体的组合，颗粒、圆柱体、球体和片状体的组合等。
优选地，步骤(a)所述待再生吸附剂来自焦化厂焦炉烟气净化中所用的吸附剂。
优选地，步骤(a)所述加热解析的温度为450℃～550℃，例如450℃、460℃、470℃、480℃、490℃、500℃、510℃、520℃、530℃、540℃或550℃等，但并不仅限于所列举的数值，该数值范围内其他未列举的数值同样适用。
作为本发明优选的技术方案，步骤(b)所述筛分在筛分装置中进行。
优选地，步骤(b)所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物。其中，粉状物的粒径可为1.7mm、1.5mm、1.3mm、1mm、0.7mm、0.5mm或0.3mm等以及更小粒径，但并不仅限于所列举的数值，该数值范围内 其他未列举的数值同样适用。例如，筛下物包括粒度＞2mm的活性炭渣和粒度小于2mm的活性碳粉。
优选地，所述粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，所述粒度＜2mm的粉状物参与配煤炼焦。
优选地，步骤(c)所述吹扫气为氮气。
优选地，步骤(c)所述解析气包括N 2、SO 2和CO；
优选地，步骤(c)中通过控制吹扫气的通入量控制解析气中SO 2的体积含量为5％～20％，例如5％、8％、10％、12％、15％、18％或20％等，但并不仅限于所列举的数值，该数值范围内其他未列举的数值同样适用，优选为10％～15％。
优选地，步骤(c)中解析气通入硫铵处理段回收硫后其CO的体积含量为10％～25％，例如10％、13％、15％、17％、20％、23％或25％等，但并不仅限于所列举的数值，该数值范围内其他未列举的数值同样适用。
优选地，步骤(c)中解析气经过净化处理后通入硫铵处理段回收硫。
作为本发明优选的技术方案，所述方法包括以下步骤：
(a)将来自焦化厂焦炉烟气净化中所用的待再生的活性炭和/或活性焦在解析塔中在450℃～550℃下进行加热解析并冷却，得到再生物料；
(b)将再生物料进行筛分得到筛上物和筛下物，所述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物，粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，所述粒度＜2mm的粉状物参与配煤炼焦；
(c)解析完成后，向解析塔中通入氮气进行吹扫后得到解析气，并通过控制吹扫气的通入量控制解析气中SO 2的体积含量为5％～20％，解析气经过净化 处理后通入硫铵处理段回收硫，然后进入焦炉作为燃料燃烧。
与现有技术相比，本发明具有以下有益效果：
本发明所述的焦炉烟气净化中吸附剂的再生系统及再生方法，主要针对焦化厂焦炉烟气过程中使用的吸附剂，吸附剂吸附脱除烟气中的SO 2、NO x、重金属、粉尘、H 2S和挥发性有机物等有害物质后进入解析塔内再生，再生工艺过程中不产生任何废物，副产物吸附剂粉(渣)应用于污水净化和焦炉炼焦，解析气回收硫后进焦炉参与燃烧；
本发明所述再生系统及再生方法解决了副产物的回收利用问题，配合活性炭吸附净化工艺可真正的实现高效清洁的烟气净化。
附图说明
图1是本发明所述的焦炉烟气净化中吸附剂的再生系统的结构示意图；
图2是本发明实施例1中所述焦炉烟气净化中吸附剂的再生系统的结构示意图；
图3是本发明实施例2中所述焦炉烟气净化中吸附剂的再生系统的结构示意图；
其中，1-解析塔，2-筛分装置，3-热源发生装置，4-硫铵处理段，5-焦炉，6-风机，7-净化装置，8-吸附塔斗提机，9-吸附剂缓冲仓。
具体实施方式
为更好地说明本发明，便于理解本发明的技术方案，下面对本发明进一步详细说明。但下述的实施例仅仅是本发明的简易例子，并不代表或限制本发明的权利保护范围，本发明保护范围以权利要求书为准。
本发明具体实施方式部分提供了一种焦炉烟气净化中吸附剂的再生系统及再生方法，如图1所示，所述系统包括解析塔1、筛分装置2、热源发生装置 3、硫铵处理段4和焦炉5；
其中，所述解析塔1顶部设有待再生吸附剂进料口，底部设有再生吸附剂出料口，所述再生吸附剂出料口与筛分装置2相连，所述解析塔1内包括位于上部的加热段和位于加热段下方的冷却段，所述加热段的热源入口连接热源发生装置3，加热段的热源出口返回热源发生装置3，冷却段的冷源入口连接冷源；所述解析塔1下部设有吹扫气入口，上部设有解析气出口，所述解析气出口连接硫铵处理段4和焦炉5。
所述方法包括以下步骤：
(a)将待再生吸附剂在解析塔1中进行加热解析并冷却，得到再生物料；
(b)步骤(b)中再生物料进行筛分得到筛上物和筛下物，所述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物参与焦化废水处理和/或配煤炼焦；
(c)解析完成后，向解析塔1中通入吹扫气进行吹扫后得到解析气，解析气通入硫铵处理段4回收硫，然后进入焦炉5作为燃料燃烧。
以下为本发明典型但非限制性实施例：
实施例1：
本实施例提供了一种焦炉烟气净化中吸附剂的再生系统及再生方法，如图2所示，所述系统包括解析塔1、筛分装置2、热源发生装置3、硫铵处理段4和焦炉5和风机6；
其中，所述解析塔1顶部设有待再生吸附剂进料口，底部设有再生吸附剂出料口，所述再生吸附剂出料口与筛分装置2相连，再生吸附剂出料口与筛分装置2之间设置卸料阀，所述解析塔1内包括位于上部的加热段和位于加热段下方的冷却段，所述加热段的热源入口连接热源发生装置3，加热段的热源入 口与热源发生装置3之间设置循环风机，加热段的热源出口返回热源发生装置3，冷却段的冷源入口连接冷源，冷源由风机6产生；所述解析塔1下部设有吹扫气入口，上部设有解析气出口，所述解析气出口连接硫铵处理段4和焦炉5；热风炉的供热介质为焦炉煤气，吸附剂为焦化厂焦炉烟气净化中所用的颗粒活性炭，所述筛分装置2为震动筛。
所述系统的处理方法包括以下步骤：
(a)将来自焦化厂焦炉烟气净化中所用的待再生的颗粒活性炭通过吸附塔斗提机8送入解析塔1中，在解析塔1中在500℃下进行加热解析并冷却，得到再生物料；
(b)将再生物料进行在筛分装置2中进行筛分，得到筛上物和筛下物，所述筛上物为再生吸附剂送入吸附剂缓冲仓9中的待吸附-解析循环利用，所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物，粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，待净化能力明显降低时再进配煤车间参与配煤炼焦，废水处理工段消纳不了的直接去配煤炼焦，所述粒度＜2mm的粉状物参与配煤炼焦；
(c)解析完成后，向解析塔1中通入氮气进行吹扫后得到解析气，并通过控制吹扫气的通入量控制解析气中SO 2的体积含量为15％，解析气通入硫铵处理段4回收硫，回收硫后的气体中CO的体积含量达到20％，其进入焦炉5作为燃料燃烧。
本实施例所述系统和方法不产生任何废物，解决了副产物的回收利用问题。
实施例2：
本实施例提供了一种焦炉烟气净化中吸附剂的再生系统及再生方法，所述 系统的结构参照实施例1中结构，区别仅在于，如图3所示，所述系统还包括净化装置7，所述位于解析气出口与硫铵处理段4之间，所述净化装置7为布袋除尘装置；热风炉的供热介质为焦炉高炉混合煤气。
所述再生方法参照实施例1中方法，区别仅在于：所述吸附剂为来自焦化厂焦炉烟气净化中所用的待再生的圆柱体活性焦；步骤(a)中解析温度为460℃；步骤(b)中粒度＞2mm的渣状物送去焦化废水处理车间，然后集中外卖给活性炭回收厂家回收或小型炉窑作燃料；步骤(c)中向解析塔1中通入氮气进行吹扫后得到解析气，并通过控制吹扫气的通入量控制解析气中SO 2的体积含量为10％，解析气经过净化装置7脱除粉尘后通入硫铵处理段4回收硫，然后进入焦炉5作为燃料燃烧。
本实施例所述系统和方法不产生任何废物，解决了副产物的回收利用问题。
实施例3：
本实施例提供了一种焦炉烟气净化中吸附剂的再生系统及再生方法，所述系统的结构参照实施例1中结构，区别仅在于，热风炉的供热介质为高炉煤气。
所述再生方法参照实施例1中方法，区别仅在于：所述吸附剂为来自焦化厂焦炉烟气净化中所用的待再生的球体活性炭；步骤(a)中解析温度为540℃；步骤(c)中向解析塔1中通入氮气进行吹扫后得到解析气，并通过控制吹扫气的通入量控制解析气中SO 2的体积含量为20％，解析气经过净化装置7脱除粉尘后通入硫铵处理段4回收硫，然后进入焦炉5作为燃料燃烧。
本实施例所述系统和方法不产生任何废物，解决了副产物的回收利用问题。
综合上述实施例可以看出，本发明所述的焦炉烟气净化中吸附剂的再生系统及再生方法，充分结合了焦化厂厂区资源优势，在保证烟气净化脱除效果的前提下，对系统中产生的废物进行回收再利用，即不产生三废又节约利用了资源，真正的实现了高效清洁的焦炉烟气净化，为焦化厂烟气净化提供了新的工艺技术支持或旧的工艺改造参考，具有非常重要的意义。
申请人声明，本发明通过上述实施例来说明本发明的详细工艺设备和工艺流程，但本发明并不局限于上述详细工艺设备和工艺流程，即不意味着本发明必须依赖上述详细工艺设备和工艺流程才能实施。所属技术领域的技术人员应该明了，对本发明的任何改进，对本发明产品各原料的等效替换及辅助成分的添加、具体方式的选择等，均落在本发明的保护范围和公开范围之内。

Claims (13)

  1. 一种焦炉烟气净化中吸附剂的再生系统，其特征在于，所述系统包括解析塔(1)、筛分装置(2)、热源发生装置(3)、硫铵处理段(4)和焦炉(5)；
    其中，所述解析塔(1)顶部设有待再生吸附剂进料口，底部设有再生吸附剂出料口，所述再生吸附剂出料口与筛分装置(2)相连，所述解析塔(1)内包括位于上部的加热段和位于加热段下方的冷却段，所述加热段的热源入口连接热源发生装置(3)，加热段的热源出口返回热源发生装置(3)，冷却段的冷源入口连接冷源；所述解析塔(1)下部设有吹扫气入口，上部设有解析气出口，所述解析气出口连接硫铵处理段(4)和焦炉(5)。
  2. 根据权利要求1所述的再生系统，其特征在于，所述筛分装置(2)筛分得到筛上物和筛下物，所述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物参与焦化废水处理和/或配煤炼焦。
  3. 根据权利要求2所述的再生系统，其特征在于，所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物。
  4. 根据权利要求3所述的再生系统，其特征在于，所述粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，所述粒度＜2mm的粉状物参与配煤炼焦。
  5. 根据权利要求1-4任一项所述的再生系统，其特征在于，所述筛分装置(2)为震动筛；
    优选地，所述再生吸附剂出料口与筛分装置(2)之间设置卸料阀。
  6. 根据权利要求1-5任一项所述的再生系统，其特征在于，所述热源发生装置(3)为热风炉，其产生温度为450℃～550℃的烟气作为解析塔(1)的热源；
    优选地，所述加热段的热源入口与热源发生装置(3)之间设置气体输送装置；
    优选地，所述气体输送装置为循环风机；
    优选地，所述热风炉的供热介质为煤气；
    优选地，所述煤气为焦炉煤气、焦炉高炉混合煤气、高炉煤气或天然气中任意一种或至少两种的组合；
    优选地，所述冷源为空气；
    优选地，所述冷源由风机(6)产生，风机(6)与冷却段的冷源入口相连。
  7. 根据权利要求1-6任一项所述的再生系统，其特征在于，所述吹扫气入口位于解析塔(1)中冷却段下方；
    优选地，所述吹扫气为氮气；
    优选地，所述吹扫气入口连接氮气产生装置；
    优选地，所述解析气出口位于解析塔(1)中加热段上方。
  8. 根据权利要求1-7任一项所述的再生系统，其特征在于，所述解析气出口与硫铵处理段(4)之间设置净化装置(7)；
    优选地，所述净化装置(7)为布袋除尘装置。
  9. 根据权利要求1-8任一项所述的再生系统，其特征在于，所述待再生吸附剂为脱硫吸附剂；
    优选地，所述脱硫吸附剂为活性炭和/或活性焦，优选为活性炭；
    优选地，所述待再生吸附剂的形状为颗粒、圆柱体、球体或片状体中任意一种或至少两种的组合；
    优选地，所述待再生吸附剂来自焦化厂焦炉烟气净化中所用的吸附剂。
  10. 一种焦炉烟气净化中吸附剂的再生方法，其特征在于，所述方法包括 以下步骤：
    (a)将待再生吸附剂在解析塔(1)中进行加热解析并冷却，得到再生物料；
    (b)将再生物料进行筛分得到筛上物和筛下物，所述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物参与焦化废水处理和/或配煤炼焦；
    (c)解析完成后，向解析塔(1)中通入吹扫气进行吹扫后得到解析气，解析气通入硫铵处理段(4)回收硫，然后进入焦炉(5)作为燃料燃烧。
  11. 根据权利要求10所述的再生方法，其特征在于，步骤(a)所述待再生吸附剂为脱硫吸附剂；
    优选地，所述脱硫吸附剂为活性炭和/或活性焦，优选为活性炭；
    优选地，步骤(a)所述待再生吸附剂的形状为颗粒、圆柱体、球体或片状体中任意一种或至少两种的组合；
    优选地，步骤(a)所述待再生吸附剂来自焦化厂焦炉烟气净化中所用的吸附剂；
    优选地，步骤(a)所述加热解析的温度为450℃～550℃。
  12. 根据权利要求10或11所述的再生方法，其特征在于，步骤(b)所述筛分在筛分装置(2)中进行；
    优选地，步骤(b)所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物；
    优选地，所述粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，所述粒度＜2mm的粉状物参与配煤炼焦；
    优选地，步骤(c)所述吹扫气为氮气；
    优选地，步骤(c)所述解析气包括N 2、SO 2和CO；
    优选地，步骤(c)中通过控制吹扫气的通入量控制解析气中SO 2的体积含量为5％～20％，优选为10％～15％；
    优选地，步骤(c)中解析气通入硫铵处理段(4)回收硫后其CO的体积含量为10％～25％；
    优选地，步骤(c)中解析气经过净化处理后通入硫铵处理段(4)回收硫。
  13. 根据权利要求10-12任一项所述的再生方法，其特征在于，所述方法包括以下步骤：
    (a)将来自焦化厂焦炉烟气净化中所用的待再生的活性炭和/或活性焦在解析塔(1)中在450℃～550℃下进行加热解析并冷却，得到再生物料；
    (b)将再生物料进行筛分得到筛上物和筛下物，所述筛上物为再生吸附剂进行吸附-解析循环利用，所述筛下物包括粒度＞2mm的渣状物和粒度＜2mm的粉状物，粒度＞2mm的渣状物送入焦化废水处理工序作为水处理吸附剂使用，所述粒度＜2mm的粉状物参与配煤炼焦；
    (c)解析完成后，向解析塔(1)中通入氮气进行吹扫后得到解析气，并通过控制吹扫气的通入量控制解析气中SO 2的体积含量为5％～20％，解析气经过净化处理后通入硫铵处理段(4)回收硫，然后进入焦炉(5)作为燃料燃烧。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111569582A (zh) * 2020-04-30 2020-08-25 安徽铭泽药业有限公司 一种中药材加工用脱硫装置
CN114260002A (zh) * 2021-11-15 2022-04-01 国能(山东)能源环境有限公司 一种活性焦解析装置及其应用

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109701357A (zh) * 2019-03-11 2019-05-03 杨松 一种VOCs废气吸附剂冷却活化用链传动篦床
CN112892511A (zh) * 2021-03-29 2021-06-04 中国华能集团清洁能源技术研究院有限公司 一种烟气多污染物协同脱除的再生系统及方法
CN114217010A (zh) * 2021-11-29 2022-03-22 北京首钢股份有限公司 一种测试脱硫脱硝用活性炭解析效果的解析系统及方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102794080A (zh) * 2012-08-30 2012-11-28 北京国电清新环保技术股份有限公司 一种焦炉烟气余热回收联合污染物综合治理方法及装置
CN102824826A (zh) * 2012-08-30 2012-12-19 北京国电清新环保技术股份有限公司 一种焦炉烟气污染物综合治理方法及装置
CN104001403A (zh) * 2014-05-06 2014-08-27 中国科学院过程工程研究所 一种活性焦/炭烟气脱硫脱硝及回收单质硫的工艺及装置
KR20140118046A (ko) * 2013-03-28 2014-10-08 현대제철 주식회사 활성탄 재생장치
CN104190388A (zh) * 2014-08-27 2014-12-10 中冶长天国际工程有限责任公司 包括余热利用的活性炭热解析方法及其装置
CN106379916A (zh) * 2016-08-30 2017-02-08 中冶华天工程技术有限公司 脱硫活性焦解析烟气资源化利用方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103657275B (zh) * 2013-12-11 2016-02-10 北京中能诺泰节能环保技术有限责任公司 双重烟气净化工艺及其净化系统
CN204503101U (zh) * 2014-11-28 2015-07-29 湖南中冶长天节能环保技术有限公司 活性炭热解析装置
CN105688873B (zh) * 2014-11-28 2018-07-24 湖南中冶长天节能环保技术有限公司 活性炭热解析方法及其装置
CN106178811B (zh) * 2015-04-29 2018-11-06 湖南中冶长天节能环保技术有限公司 防止解析气体输出管道堵塞的活性炭热解析方法及其装置

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102794080A (zh) * 2012-08-30 2012-11-28 北京国电清新环保技术股份有限公司 一种焦炉烟气余热回收联合污染物综合治理方法及装置
CN102824826A (zh) * 2012-08-30 2012-12-19 北京国电清新环保技术股份有限公司 一种焦炉烟气污染物综合治理方法及装置
KR20140118046A (ko) * 2013-03-28 2014-10-08 현대제철 주식회사 활성탄 재생장치
CN104001403A (zh) * 2014-05-06 2014-08-27 中国科学院过程工程研究所 一种活性焦/炭烟气脱硫脱硝及回收单质硫的工艺及装置
CN104190388A (zh) * 2014-08-27 2014-12-10 中冶长天国际工程有限责任公司 包括余热利用的活性炭热解析方法及其装置
CN106379916A (zh) * 2016-08-30 2017-02-08 中冶华天工程技术有限公司 脱硫活性焦解析烟气资源化利用方法

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111569582A (zh) * 2020-04-30 2020-08-25 安徽铭泽药业有限公司 一种中药材加工用脱硫装置
CN114260002A (zh) * 2021-11-15 2022-04-01 国能(山东)能源环境有限公司 一种活性焦解析装置及其应用

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