WO2024239727A1 - Système de réacteur scr capable de réaliser une régénération in situ et son procédé d'utilisation - Google Patents

Système de réacteur scr capable de réaliser une régénération in situ et son procédé d'utilisation Download PDF

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Publication number
WO2024239727A1
WO2024239727A1 PCT/CN2024/077514 CN2024077514W WO2024239727A1 WO 2024239727 A1 WO2024239727 A1 WO 2024239727A1 CN 2024077514 W CN2024077514 W CN 2024077514W WO 2024239727 A1 WO2024239727 A1 WO 2024239727A1
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WO
WIPO (PCT)
Prior art keywords
flue gas
regeneration
scr reactor
partition
gas inlet
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2024/077514
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English (en)
Chinese (zh)
Inventor
陈廷
银登国
杜文韬
陈倬
武娟
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Dongfangboiler Group Co Ltd
Original Assignee
Dongfangboiler Group Co Ltd
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Application filed by Dongfangboiler Group Co Ltd filed Critical Dongfangboiler Group Co Ltd
Publication of WO2024239727A1 publication Critical patent/WO2024239727A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8609—Sulfur oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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

Definitions

  • the present invention relates to the technical field of environmental protection denitration, and in particular to an in-situ regenerable SCR reactor system and a method for using the same.
  • SCR Selective catalytic reduction
  • the most widely used temperature for SCR catalysts is 280-450°C. At this temperature, most of the ammonium bisulfate is in gaseous state, which has little effect on the catalyst.
  • the flue gas temperature is generally lower than 280°C after desulfurization and dust removal, and medium and low temperature SCR processes are often used for denitrification.
  • the medium and low temperature SCR reaction system most of the ammonium bisulfate is in liquid state, has strong adhesion, and is very easy to adhere to the surface of the catalyst to form contamination.
  • liquid ammonium bisulfate is easy to adsorb dust in the flue gas, which expands the contamination area, resulting in a reduction in the effective contact area between the catalyst and the flue gas, affecting the catalytic reaction process, reducing the catalytic efficiency, and causing problems such as NOx and ammonia escape emissions not meeting the standards.
  • a regeneration system is usually provided to achieve in-situ regeneration of the catalyst.
  • the patent with publication number CN107913598A discloses an online regeneration system and regeneration method for SCR low temperature denitration catalyst in a domestic waste incineration plant. By setting a regeneration fan, a heating furnace for regeneration, a regeneration pipeline and a baffle, the in-situ regeneration of the SCR catalyst is achieved.
  • the regeneration process requires the flue gas to be completely bypassed. During the regeneration period, the SCR reactor completely loses its denitration function, and the NOx emitted from the flue gas cannot meet the standard.
  • the patent with publication number CN208082232U discloses a low-temperature SCR denitration reactor that can be maintained online. By partitioning the SCR reactor, the SCR catalyst can be regenerated online. The regeneration process does not require flue gas bypass and the operation of the denitration device does not need to be stopped. Nitrogen oxides can be discharged up to standard during maintenance. However, after the catalyst in the SCR reactor has been running for a long time, ammonium bisulfate and particulate matter will be deposited on the surface of the catalyst. During the regeneration process, the catalyst is heated by high-temperature air (or flue gas) to vaporize the ammonium bisulfate attached to the catalyst surface and decompose it into sulfide and ammonia. The particulate matter adsorbed by the ammonium bisulfate will also be released. If the regenerated exhaust gas is directly discharged into the chimney, it will cause sulfide and ammonia to escape and particulate matter to exceed the standard.
  • the present invention provides an in-situ regenerable SCR reactor system and a method for using the same, which solves the problems of sulfide and ammonia escape and excessive particulate matter emissions in flue gas caused by gasification and decomposition of ammonium bisulfate in the prior art.
  • An in-situ regenerative SCR reactor system comprises a desulfurization tower and an SCR reactor which are connected in sequence along the flow direction of original flue gas, and also comprises a flue gas heater, a regeneration fan, an induced draft fan, a regeneration flue gas inlet valve, a waste gas exhaust valve, and a flue gas heat exchanger.
  • the SCR reactor is divided into j separate partitions, each partition is independent from the inlet to the outlet, each partition is connected with an original flue gas inlet and outlet baffle, a regeneration flue gas inlet and outlet valve, the induced draft fan, the regeneration flue gas inlet valve, the regeneration fan, the flue gas heat exchanger, the flue gas heater, and the regeneration flue gas inlet and outlet valves of each partition are connected in sequence, and the regeneration flue gas inlet and outlet valves of each partition, the flue gas heat exchanger, the waste gas exhaust valve, and the original flue gas inlet of the desulfurization tower are connected in sequence; wherein j ⁇ 2 and j is an integer.
  • it also includes a dust collector, and the desulfurization tower, the dust collector, and the SCR reactor are connected in sequence along the original flue gas flow direction.
  • it also includes an ammonia injection grid, a desulfurization tower, a dust collector, an ammonia injection grid, and an SCR reactor which are connected in sequence along the original flue gas flow direction.
  • the SCR reactor is divided into j separate partitions by the vertical partition.
  • the flue gas heater is one or more of an electric heater, a steam heater, and a hot air furnace.
  • it also includes a chimney, and the SCR reactor, the induced draft fan and the chimney are connected in sequence.
  • a method for using an in-situ regenerable SCR reactor system using the in-situ regenerable SCR reactor system, when the catalyst in the i-th partition is contaminated and needs to be regenerated, the original flue gas inlet and outlet dampers of the i-th partition are adjusted to a closed state, and the inlet and outlet dampers of the other partitions remain open;
  • the purified flue gas is heated to the regeneration temperature by the flue gas heat exchanger and the flue gas heater, and then enters the i-th partition.
  • the ammonium bisulfate attached to the catalyst in the i-th partition is gasified and decomposed into sulfide and ammonia.
  • the particulate matter adsorbed by the ammonium bisulfate is also desorbed and released.
  • the inlet and outlet baffles of the partition are closed, and the partition is repaired, while other partitions operate normally.
  • the temperature required for regeneration is 350°C to 400°C.
  • the present invention has the following beneficial effects:
  • the SCR reactor of the present invention is divided into zones, and the number of zones is not less than 2.
  • the specific number of zones is reasonably determined based on the size of the reactor and the operating conditions of the unit, so that the SCR reactor can operate continuously from low load to high load of the unit, and the catalyst can be regenerated without stopping the unit.
  • the exhaust point of the catalyst regeneration pipeline of the present invention is located before the desulfurization and dust removal unit.
  • the exhaust gas generated during the catalyst regeneration process does not need to be pretreated and is directly sent to the desulfurization and dust removal unit through the pipeline. It is discharged after flue gas purification, and the catalyst regeneration exhaust gas treatment is completed safely, environmentally friendly and quickly, ensuring that the flue gas meets the emission standards during the catalyst regeneration process.
  • the flue gas heater of the present invention adopts a grouping design and a regeneration fan variable frequency regulation, which can meet the heat load and air volume requirements of multiple catalyst partitions for simultaneous regeneration.
  • the present invention uses a flue gas heat exchanger to increase the clean flue gas temperature, save energy consumption, reduce the flue gas temperature after regeneration, and avoid high-temperature flue gas entering the absorption tower causing uneven flue gas temperature that affects desulfurization efficiency and equipment safety.
  • FIG1 is a schematic structural diagram of an in-situ regenerable SCR reactor system according to the present invention.
  • the present invention proposes an in-situ regenerated SCR reactor system to solve the problems of sulfide, ammonia escape and excessive particulate matter emissions in flue gas caused by ammonium bisulfate gasification and decomposition during the regeneration process of the SCR catalyst.
  • the present invention can achieve in-situ regeneration of the SCR catalyst without stopping the machine, affecting the denitrification efficiency and ensuring that the sulfide and particulate matter emissions in the flue gas do not exceed the standard.
  • the present invention has the advantages of reasonable design, high working efficiency, convenient maintenance and reliable system.
  • the in-situ regeneration SCR reactor system designed by the present invention is composed of the following parts: an SCR reactor 4 for providing a denitration reaction site, a flue gas heater (electric heater, steam heater, hot blast furnace, etc.) 5 for providing a heat source, a regeneration fan 6 for providing kinetic energy, a pipeline system and an instrument valve.
  • the gas used in the regeneration process of the in-situ regeneration SCR reactor system designed by the present invention is clean flue gas, the clean flue gas inlet point is located after the induced draft fan 7, and the flue gas exhaust point after regeneration is located before the dust collector 2 and the desulfurization tower 1.
  • the high-temperature flue gas after regeneration exchanges heat with the low-temperature clean flue gas through the flue gas heat exchanger 15, thereby increasing the clean flue gas temperature and reducing the energy consumption of the flue gas heater 5.
  • the SCR reactor 4 is divided into 1, 2, ... j, a total of j areas (j ⁇ 2) by vertical partitions, and each partition inlet and outlet flue is provided with an electric baffle (i partition original flue gas inlet and outlet baffle 13, j partition original flue gas inlet and outlet baffle 14), which is used to isolate the corresponding partition from the original flue gas during regeneration or maintenance.
  • the regeneration pipelines connected to each partition are equipped with valves (regeneration flue gas inlet and outlet valves 11 for partition i, regeneration flue gas inlet and outlet valves 12 for partition j), which cooperate with the electric dampers at the inlet and outlet of the corresponding partitions (original flue gas inlet and outlet dampers 13 for partition i, original flue gas inlet and outlet dampers 14 for partition j) to realize automatic switching of the corresponding partition operation, regeneration, maintenance and other working conditions.
  • valves regeneration flue gas inlet and outlet valves 11 for partition i, regeneration flue gas inlet and outlet valves 12 for partition j
  • the present invention divides the SCR reactor into zones and reasonably sets the air inlet and exhaust points of the catalyst regeneration pipeline, thereby mainly achieving the following beneficial effects:
  • the SCR reactor is partitioned, with the number of partitions not less than 2.
  • the specific number of partitions is reasonably determined based on the reactor size and the unit operating conditions, so that the SCR reactor can operate continuously from low load to high load of the unit and the catalyst can be regenerated without stopping the unit.
  • the exhaust point of the catalyst regeneration pipeline is located in front of the desulfurization and dust removal unit.
  • the exhaust gas generated during the catalyst regeneration process does not need to be pretreated and is directly sent to the desulfurization and dust removal unit through the pipeline. It is discharged after flue gas purification, and the catalyst regeneration exhaust gas treatment is completed safely, environmentally friendly and quickly to ensure that the flue gas emissions meet the standards during the catalyst regeneration process.
  • the flue gas heater adopts a group design and the regeneration fan is frequency-controlled to meet the heat load and air volume requirements of multiple catalyst partitions for simultaneous regeneration.
  • the flue gas heat exchanger is used to increase the clean flue gas temperature, save energy, reduce the flue gas temperature after regeneration, and avoid the high-temperature flue gas entering the absorption tower causing uneven flue gas temperature and affecting the desulfurization efficiency and equipment safety.
  • the reactor of the present invention is divided into zones, and isolation baffles are arranged before and after each zone.
  • the reactor of the present invention is provided with regeneration air at each partition inlet, adopts the clean flue gas after denitration, and is provided with a regeneration fan, a flue gas heat exchanger and a flue gas heater to introduce the heated clean flue gas into the reactor, and the regeneration air interface is located behind the reactor baffle door.
  • Each partition outlet of the reactor of the present invention is connected to the inlet of the desulfurization device, and the regenerated waste gas is purified through the desulfurization, dust removal and denitration devices.
  • Example 1 As shown in FIG1 , as a further optimization of Example 1, based on Example 1, this embodiment also includes the following technical features:
  • the SCR reactor 4 is divided into j zones, 1, 2, ...j, by vertical partitions 16. Each zone inlet and outlet flue is provided with an electric damper (i zone original flue gas inlet and outlet damper 13, j zone original flue gas inlet and outlet damper 14), and each zone is independent from the inlet to the outlet of the SCR reactor 4.
  • the inlet and outlet dampers of the SCR reactor 4 i zone original flue gas inlet and outlet damper 13, j zone original flue gas inlet and outlet damper 14
  • the regeneration flue gas inlet valve 9 and the exhaust gas exhaust valve 10 on the regeneration pipeline system are all closed, and the flue gas heater 5 and the regeneration fan 6 do not work.
  • the unpurified raw flue gas passes through the desulfurization tower 1, the dust collector 2, the ammonia injection grid 3, and the SCR reactor 4 in turn, and is sent to the chimney 8 by the induced draft fan 7 and discharged into the atmosphere.
  • the catalyst of the i-th partition (i ⁇ j) is contaminated, the denitrification efficiency is reduced, and the catalyst needs to be regenerated. Then adjust the original flue gas inlet and outlet dampers 13 of the i-th partition to the closed state, and the inlet and outlet dampers of the other partitions remain open. Open the regenerated flue gas inlet valve 9 and the exhaust gas exhaust valve 10, open the regenerated flue gas inlet and outlet valve 11 of the i-th partition, and keep the electric valves of the other partitions closed, and start the flue gas heater 5 and the regeneration fan 6.
  • the purified flue gas is heated to the regeneration temperature (350°C to 400°C) required for regeneration by the flue gas heat exchanger 15 and the flue gas heater 5, and enters the i-th partition.
  • the ammonium bisulfate attached to the catalyst of the i-th partition is gasified and decomposed at high temperature, and the ammonium bisulfate is decomposed into sulfide and ammonia.
  • the particulate matter adsorbed by the ammonium bisulfate will also be desorbed and released.
  • the flue gas generated by decomposition and release is heat exchanged with the clean flue gas extracted by the regeneration fan 6 through the flue gas heat exchanger 15, mixed with the original flue gas after cooling, and re-introduced into the dust collector 2 and the desulfurization tower 1. After the flue gas purification is completed, it is introduced into the chimney 8 by the induced draft fan 7 and discharged into the atmosphere.
  • the flue gas heater adopts a group design and the regeneration fan is frequency-controlled, which can meet the heat load and air volume requirements of multiple catalyst partitions for simultaneous regeneration. When regeneration needs to be completed in a short time, multiple catalyst bins can be regenerated simultaneously.
  • the regenerated flue gas inlet valve 9 and the waste gas exhaust valve 10 are preferably electric valves
  • the i-zone regenerated flue gas inlet and outlet valves 11 and the j-zone regenerated flue gas inlet and outlet valves 12 are preferably electric valves
  • the i-zone original flue gas inlet and outlet baffles 13 and the j-zone original flue gas inlet and outlet baffles 14 are preferably electric baffles.
  • the present invention can be preferably implemented.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

L'invention concerne un système de réacteur SCR capable de réaliser une régénération in situ et son procédé d'utilisation. Un réacteur SCR est divisé en j zones indépendantes ; toutes les zones sont mutuellement indépendantes entre une entrée et une sortie ; chaque zone étant raccordée à un déflecteur d'entrée et de sortie de gaz de combustion d'origine, et une soupape d'entrée et de sortie de gaz de combustion régénéré ; un ventilateur à tirage induit (7), une soupape d'entrée de gaz de combustion régénéré (9), un ventilateur de régénération (6), un échangeur de chaleur de gaz de combustion (15), un dispositif de chauffage de gaz de combustion (5), et la soupape d'entrée et de sortie de gaz de combustion régénéré de chaque zone sont en communication séquentielle ; la soupape d'entrée et de sortie de gaz de combustion régénéré de chaque zone, l'échangeur de chaleur de gaz de combustion (15), une soupape d'échappement de gaz résiduaire (10) et une entrée de gaz de combustion d'origine d'une colonne de désulfuration (1) sont en communication séquentielle.
PCT/CN2024/077514 2023-05-23 2024-02-19 Système de réacteur scr capable de réaliser une régénération in situ et son procédé d'utilisation Ceased WO2024239727A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202310582519.4 2023-05-23
CN202310582519.4A CN116531937A (zh) 2023-05-23 2023-05-23 一种可原位再生的scr反应器系统及其使用方法

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WO2024239727A1 true WO2024239727A1 (fr) 2024-11-28

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Publication number Priority date Publication date Assignee Title
CN116531937A (zh) * 2023-05-23 2023-08-04 东方电气集团东方锅炉股份有限公司 一种可原位再生的scr反应器系统及其使用方法

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CN108014613A (zh) * 2016-11-02 2018-05-11 煤科院节能技术有限公司 一种基于炭材料氧化脱硝的半干式烟气净化系统及方法
CN208066118U (zh) * 2017-12-20 2018-11-09 北京中冶设备研究设计总院有限公司 一种焦炉烟气脱硫脱硝除尘综合治理装置
EP3840861A1 (fr) * 2018-08-22 2021-06-30 Shell Internationale Research Maatschappij B.V. Procédé de réduction catalytique sélective et procédé de régénération d'un catalyseur désactivé du procédé
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EP2486971A1 (fr) * 2011-02-11 2012-08-15 Lab Sa Procédé de régénération thermique en ligne d'un catalyseur de dénitrification de fumées, et installation d'épuration des fumées permettant de mettre en oeuvre ce procédé
CN106334444A (zh) * 2016-11-17 2017-01-18 西南化工研究设计院有限公司 一种焦炉烟气低温连续脱硝工艺及其反应器
CN208082232U (zh) * 2018-03-12 2018-11-13 杭州双良中荷环保科技有限公司 一种可在线维护的低温scr脱硝反应器
CN111151130A (zh) * 2020-02-27 2020-05-15 东方电气集团东方锅炉股份有限公司 具有在线再生的垃圾焚烧炉scr烟气脱硝系统及其脱硝方法
CN211936382U (zh) * 2020-02-27 2020-11-17 东方电气集团东方锅炉股份有限公司 具有在线再生的垃圾焚烧炉scr烟气脱硝系统
CN116531937A (zh) * 2023-05-23 2023-08-04 东方电气集团东方锅炉股份有限公司 一种可原位再生的scr反应器系统及其使用方法

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