CN116764377A - Ultralow emission treatment system and method for tail gas of oil-fired boiler - Google Patents

Ultralow emission treatment system and method for tail gas of oil-fired boiler Download PDF

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Publication number
CN116764377A
CN116764377A CN202310850341.7A CN202310850341A CN116764377A CN 116764377 A CN116764377 A CN 116764377A CN 202310850341 A CN202310850341 A CN 202310850341A CN 116764377 A CN116764377 A CN 116764377A
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China
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flue gas
treatment
unit
denitration
heat exchanger
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CN202310850341.7A
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Inventor
许璐
王小立
杨海霞
沈滨
田高峰
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Beijing Longyuan Environmental Engineering Co ltd
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Beijing Longyuan Environmental Engineering Co ltd
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    • 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
    • B01D53/005—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 heat treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
    • B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
    • 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
    • B01D53/343—Heat recovery
    • 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
    • B01D53/346—Controlling the process
    • 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/90—Injecting reactants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B01D2252/1035—Sea water
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/30—Technologies for a more efficient combustion or heat usage

Abstract

The application discloses an ultralow emission treatment system and a treatment method for tail gas of a fuel oil boiler, and relates to the technical field of environmental protection tail gas treatment, wherein the ultralow emission treatment system comprises a dust removal unit, a heating unit, a denitration unit, a heat recovery unit, a draught fan, a desulfurization unit and a flue gas discharge unit which are sequentially communicated through pipelines, and the dust removal unit is used for performing dust removal treatment operation on raw flue gas; the heating unit is used for heating the flue gas subjected to dust removal treatment; the denitration unit is used for carrying out denitration treatment on the flue gas subjected to the heating treatment; the heat recovery unit is used for cooling and recovering heat of the flue gas subjected to denitration treatment; the induced draft fan is used for providing power for the transmission of the flue gas in the pipeline; a desulfurization unit for performing desulfurization treatment operation; and the smoke exhaust unit is used for exhausting smoke. The application can reduce energy consumption and recover heat during the tail gas treatment of the oil-fired boiler, and simultaneously reduce emission of pollutants, thereby achieving ultra-low emission of the pollutants.

Description

Ultralow emission treatment system and method for tail gas of oil-fired boiler
The application discloses a divisional application of a system and a method for treating ultralow emission of tail gas of a fuel oil boiler, wherein the application number of the main application is 202210614635.5, and the application date is 2022.05.30.
Technical Field
The application relates to the technical field of environmental protection tail gas treatment, in particular to an ultralow emission treatment system and method for tail gas of an oil-fired boiler.
Background
In recent years, the flue gas treatment of China coal-fired power plants has reached a higher level. The treatment technology of the flue gas pollutants of the coal-fired power plant also reaches higher technical level, and a set of mature process technology route applicable to ultralow emission of the coal-fired power plant is formed, and smoke dust and SO are generated 2 、NO x The discharge concentration of the pollutants can be respectively treated to 5mg/Nm 3 、35mg/Nm 3 、50mg/Nm 3 The following is given. Aiming at the emission of the flue gas pollutants of the oil-fired boiler, the flue gas pollutant treatment technology of the oil-fired boiler cannot be completely duplicated due to the fact that the combustion conditions, the flue gas components, the flue gas parameters and the like of the oil-fired boiler are greatly different from those of the oil-fired boiler. For oil-fired boilerThe flue gas pollutant treatment of the furnace, especially the standard for dealing with 'ultra-low emission', does not form a unified process technology route and system integration scheme, is still in a fumbling stage, and the corresponding standard and specification also need to be further perfected.
The treatment of the flue gas pollutants of the coal-fired boiler of the power plant is carried out by combining the flue gas pollution of the coal-fired boiler with each temperature window of the flue gas system, and a medium-temperature SCR denitration-heat exchange device-electrostatic (bag) dust remover-wet desulfurization tower system is generally adopted, so that a set of mature process technical route is formed. However, the exhaust gas temperature of the oil-fired boiler, especially the industrial oil-fired boiler with smaller capacity is generally below 200 ℃, and the temperature window which is similar to the coal-fired boiler and suitable for each treatment unit, especially the medium-temperature SCR denitration unit, is not available, so that the treatment system of the flue gas of the coal-fired boiler is not suitable for the flue gas treatment of the oil-fired boiler.
Other industries also correspondingly export relevant technical routes for treating the smoke pollutants. For example, patent number CN212974720U, named "a low emission system of coke oven flue gas" provides an ultra-low emission method for treating pollutants in coke oven flue gas, and adopts a system integration mode of "low-temperature SCR denitration-SDS dry desulfurization-bag-type dust remover". However, the treatment of the flue gas of the oil-fired boiler cannot be simply applied to the scheme, and the low-temperature SCR denitration technology is generally suitable for low SO 2 The flue gas of content can not adapt to the high sulfur flue gas characteristic of oil boiler, simultaneously, SCR denitration is as the first link of pollutant desorption, and substances such as peculiar tar in the oil boiler flue gas extremely easily cause the jam and the inefficacy of SCR catalyst, influence the life-span of catalyst, lead to denitration efficiency's decline. The coke oven flue gas has the requirements on the flue gas temperature after desulfurization due to the special process production requirements, is generally not lower than 130 ℃, is more suitable for SDS dry desulfurization, has no special temperature requirements on flue gas treatment and emission of a fuel oil boiler, and adopts NaHCO for SDS dry desulfurization 3 As a desulfurizing agent, the flue gas SO is relatively high in operation cost and unsuitable for being used for a fuel oil boiler 2 And (5) processing.
In addition, the patent number is CN106268235A, the name is a special oil field fuel oil steam injection boiler tail gas desulfurization and denitrification treatment systemThe tail gas desulfurization and denitrification treatment system for the oil-fired boiler is provided 2 With NO x Can respectively reach 200mg/Nm 3 With 250mg/Nm 3 The emission concentration requirement of the gas turbine is a certain gap from the ultra-low emission, and the technical scheme only has desulfurization and denitrification and has no dust removal system.
Disclosure of Invention
The application provides an ultralow emission treatment system and a treatment method suitable for tail gas of a fuel oil boiler, which are used for reducing energy consumption, recovering heat and reducing emission pollutants when treating the tail gas of the fuel oil boiler.
In order to achieve the above object, the present application provides the following solutions:
the system comprises a DCS automatic control unit, a dust removing unit, a heating unit, a denitration unit, a heat recovery unit, an induced draft fan, a desulfurization unit and a flue gas discharge unit, wherein the DCS automatic control unit is used for performing program control on a system flow, and the dust removing unit, the heating unit, the denitration unit, the heat recovery unit, the induced draft fan, the desulfurization unit and the flue gas discharge unit are sequentially communicated through pipelines;
the dust removing unit is used for collecting raw flue gas exhausted by the oil-fired boiler and carrying out dust removing treatment operation on the raw flue gas so as to reduce the concentration of smoke dust to 10mg/Nm 3 The following are set forth;
the heating unit comprises a heat exchanger and a hot blast stove which are sequentially connected; the heat exchanger is used for carrying out primary heating treatment on the clean flue gas subjected to dust removal treatment, and the primary heating is controlled at 200-270 ℃; the hot blast stove is used for carrying out secondary heating treatment on the clean flue gas subjected to primary heating, and the secondary heating is controlled at 310-350 ℃;
the denitration unit comprises a reducing agent injection device connected with a flue of the hot blast stove and an SCR denitration reactor connected with the tail end of the flue of the hot blast stove, and the denitration adopts a medium-temperature SCR denitration technology; the reducing agent injection device adopts a double-fluid spray gun to inject ammonia water, the ammonia water is gasified at high temperature and then fully mixed with the flue gas, and the mixture enters the SCR denitration reactor to be subjected to flue gas denitration treatment, so that NO x The concentration is reduced to 50mg/Nm 3 The following are set forth; the exhaust port of the SCR denitration reactor is communicated with the second air inlet of the heat exchanger, and is subjected to denitrationPerforming primary cooling treatment on the flue gas subjected to the nitrate treatment;
the heat recovery unit is used for cooling and recovering heat of the flue gas subjected to denitration treatment; the heat recovery unit comprises a finned tube heat exchanger; the fin tube heat exchanger is used for carrying out secondary cooling treatment on the flue gas subjected to denitration treatment, and the secondary cooling is controlled in a range that the temperature is lower than 140 ℃ and is higher than the acid dew point of the flue gas; the heat recovered by the finned tube heat exchanger is used for heating fuel oil and water supply;
the induced draft fan is used for providing power for transmitting the smoke in the pipeline and controlling the smoke pressure value in the system;
the desulfurization unit is used for acquiring the flue gas transmitted by the induced draft fan and carrying out desulfurization treatment operation on the flue gas SO as to enable SO (sulfur-doped oxygen) 2 The concentration is reduced to 35mg/Nm 3 The following are set forth; the desulfurization unit comprises a wet desulfurization absorption tower communicated with an exhaust port of the induced draft fan;
the flue gas discharge unit is used for discharging the flue gas treated by the system outwards; the flue gas exhaust unit is internally provided with a flue gas monitoring unit which is used for detecting whether the content of pollutants in the flue gas accords with the emission standard or not and monitoring the smoke dust and SO in the flue gas in real time 2 、NO x Is transmitted to the DCS automatic control unit in real time.
Optionally, the dust removing unit comprises a bag type dust remover; the outlet of the ash bucket of the bag type dust collector is connected with a pneumatic ash conveying device, and fly ash in the ash bucket is sprayed into a flue of the bag type dust collector and used for adsorbing tar in the fed raw flue gas; a plurality of filter bags are uniformly distributed in the bag type dust collector and are used for filtering smoke dust, and a back blowing device is arranged at the top of the bag type dust collector and is used for blowing the smoke dust and the coal ash adsorbed with tar into an ash bucket at regular time; the clean flue gas is exhausted through an exhaust port located at the top of the bag house.
Optionally, the heat exchanger adopts a heat pipe type, and a first air inlet of the heat exchanger is communicated with an air outlet of the bag type dust collector;
the hot blast stove adopts a flue direct combustion type, and an air inlet of the hot blast stove is communicated with a first air outlet of the heat exchanger.
Optionally, an exhaust port of the SCR denitration reactor is communicated with a second air inlet of the heat exchanger;
the air inlet of the finned tube heat exchanger is communicated with the second air outlet of the heat exchanger.
Optionally, two layers of catalysts are arranged up and down in the SCR denitration reactor, and the catalysts are honeycomb type or plate type catalysts.
Optionally, the induced draft fan adopts a variable frequency centrifugal fan.
Optionally, glass flakes are arranged in the wet desulfurization absorption tower, and a demister is arranged at the top of the wet desulfurization absorption tower and is used for removing fog drops in the flue gas.
In order to achieve the above purpose, the present application also provides the following technical solutions:
the ultralow emission treatment method of the tail gas of the oil-fired boiler adopts an ultralow emission treatment system of the tail gas of the oil-fired boiler for treatment, and comprises the following steps:
will contain SO 2 、NO x And the flue gas of the oil-fired boiler with the smoke dust is introduced into a bag type dust collector for dust removal treatment, so that the concentration of the smoke dust is reduced to 10mg/Nm 3 The following are set forth;
introducing the clean flue gas subjected to dust removal treatment into a heat exchanger, primarily heating to 200-270 ℃, and then introducing into a hot blast stove to secondarily heat to 310-350 ℃;
ammonia water is injected into the flue gas after the two heating treatments, the flue gas and the ammonia water after the high temperature gasification are evenly mixed, then the flue gas is introduced into an SCR denitration reactor, denitration reaction is carried out under the action of a medium temperature denitration catalyst, and NO is obtained x Conversion to N 2 And H 2 O, so that NO x The concentration is reduced to 50mg/Nm 3 The following are set forth;
the flue gas after denitration and purification is led into a heat exchanger again for primary cooling, the temperature is reduced to 240-280 ℃, and then is led into a finned tube heat exchanger for heat recovery, so that the flue gas is secondarily cooled to less than 140 ℃;
the flue gas subjected to the twice cooling treatment is led into a wet desulfurization absorption tower for desulfurization treatment, SO that SO 2 The concentration is reduced to 35mg/Nm 3 The following are set forth;
and the purified flue gas is discharged after flue gas detection.
According to the specific embodiment provided by the application, the application discloses the following technical effects:
the application is suitable for the ultralow emission treatment system and the treatment method of the tail gas of the oil-fired boiler, and the dust removal unit, the heating unit, the denitration unit, the heat recovery unit, the induced draft fan, the desulfurization unit and the flue gas discharge unit which are sequentially communicated are arranged, so that the system reasonably integrates according to the chemical reaction principle and the heat utilization rule, reduces the energy consumption and the heat recovery to the maximum extent, and accords with the overall thought of energy conservation and emission reduction while reducing emission pollutants. The flue gas is heated to the reaction temperature by the heating unit for twice and then is introduced with the reducing agent for uniform mixing and reduction, so that the flue gas reaches the adaptation temperature during the denitration reaction, an expensive low-temperature catalyst is not required to be equipped, and only a small amount of necessary fuel, an inexpensive common desulfurizing agent and a reducing agent are required, so that the operation cost is low. The exhaust port of the SCR denitration reactor is communicated with the second air inlet of the heat exchanger, the flue gas after denitration treatment is subjected to primary cooling treatment, and the flue gas is subjected to secondary cooling through the heat recovery unit, so that unnecessary loss of heat is reduced, and the utilization rate of waste heat resources is improved. The induced draft fan is arranged between the heat recovery unit and the desulfurization unit, and the position is a low-dust, low-temperature and low-corrosion area, so that the material selection of the induced draft fan does not need to consider factors such as wear resistance, high temperature resistance, corrosion resistance and the like, the investment cost is low, and the service life of equipment is long.
In addition, the dust removal unit reduces the smoke concentration to 10mg/Nm 3 The denitration unit will be described below as NO x The concentration is reduced to 50mg/Nm 3 The desulfurization unit subjects SO to the following 2 The concentration is reduced to 35mg/Nm 3 In the following, the treatment of ultralow emission of the flue gas pollutants of the oil-fired boiler is achieved, the method can be flexibly suitable for different fuel oil products, has universal applicability particularly for oil products with different sulfur content and tar content, can be suitable for wider unit load change, and can realize flue gas under all working conditionsUltra low emission treatment. The application is suitable for desulfurization, denitration and dust removal treatment of tail gas of the oil-fired boiler, so that the tail gas can reach the standard of ultra-low emission, and the operation cost is low.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions of the prior art, the drawings that are needed in the embodiments will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a general frame diagram of one embodiment of an ultra-low emission treatment system for exhaust gas of an oil-fired boiler of the present application;
FIG. 2 is a schematic diagram of the overall connection relationship of the tail gas ultra-low emission treatment system of the oil-fired boiler;
FIG. 3 is a flow chart of the method for treating ultralow emission of tail gas of the oil-fired boiler.
Symbol description:
1-oil boiler, 2-bag dust collector, 21-ash bucket, 22-back blowing device, 3-heat exchanger, 4-hot-blast furnace, 5-SCR denitration reactor, 51-catalyst, 6-fin tube heat exchanger, 7-draught fan, 8-wet desulfurization absorption tower, 81-defroster, 9-chimney, 10-double fluid spray gun.
Detailed Description
The following description of the embodiments of the present application will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present application, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.
The smoke components of the oil-fired boiler are very different from those of the coal-fired boiler of the power plant and the coke oven, and the components are complex. The smoke content in the tail gas of the oil-fired boiler is generally low and is about 200-500mg/Nm 3 Far lower than the coal-fired boiler of the power plantTherefore, the existing oil-fired boilers are not provided with tail gas dust removal devices. NO according to different oil products and combustion conditions x At a concentration of about 300-700mg/Nm 3 ，SO 2 The concentration is 600-5000mg/Nm 3 Unequal, a wide range of variation. Meanwhile, unavoidable incomplete combustion of fuel can lead to the existence of a small amount of tar, fine floccules and other substances with higher viscosity in the flue gas, and the treatment of the substances is also an important point of the system.
The exhaust temperature of the oil-fired boiler is generally 160-200 ℃, so that a reasonable integrated design is carried out on the exhaust flue gas treatment system of the oil-fired boiler at the temperature, and comprehensive utilization and recovery energy conservation of heat are considered.
In combination with the temperature interval and the component characteristics of the flue gas exhausted by the oil-fired boiler, in the flue gas treatment process, if denitration treatment is carried out first, viscous substances such as tar in the flue gas are very easy to cause the blockage and failure of the SCR denitration catalyst, the service life of the catalyst is influenced, and the denitration efficiency is reduced. If desulfurization treatment is performed first, the temperature of the flue gas is greatly reduced by wet desulfurization, the outlet temperature after desulfurization is only 30-50 ℃, and the requirement on the subsequent treatment unit such as denitration treatment can be met by heating treatment due to the higher requirement on the subsequent treatment temperature, so that energy waste can be caused, and the desulfurization unit is suitable to be arranged at the tail end of the system.
The system selects to carry out dust removal treatment firstly, and simultaneously removes tar and other substances, thereby avoiding adhesion and blockage of downstream equipment.
Fig. 1 is a frame overview of an embodiment of an ultralow emission treatment system for tail gas of an oil-fired boiler, which comprises a DCS automatic control unit for performing program control on a system flow, and further comprises a dust removal unit, a heating unit, a denitration unit, a heat recovery unit, an induced draft fan, a desulfurization unit and a flue gas discharge unit which are sequentially connected in a pipeline. The dust removing unit is used for collecting raw flue gas exhausted by the oil-fired boiler and carrying out dust removing treatment operation on the raw flue gas. The heating unit is used for heating the flue gas subjected to dust removal treatment so as to reach a temperature threshold value for denitration treatment of the flue gas. The denitration unit is used for carrying out denitration treatment on the flue gas after the heating treatment. The heat recovery unit is used for cooling and recovering heat of the flue gas subjected to denitration treatment; the induced draft fan is used for providing power for transmitting the flue gas in the pipeline, controlling the flue gas pressure value in the system, and the desulfurization unit is used for acquiring the flue gas transmitted by the induced draft fan and carrying out desulfurization treatment operation on the flue gas. The flue gas exhaust unit is used for exhausting the flue gas processed by the system outwards, and a flue gas monitoring unit is arranged in the flue gas exhaust unit and used for detecting whether the content of pollutants in the flue gas accords with the emission standard.
In the specific implementation process of the system, the dust removing unit adopts a bag type dust remover 2, and the temperature of the flue gas at the outlet of the oil-fired boiler 1 is about 160-200 ℃, so that the flue gas is firstly introduced into the bag type dust remover 2, the adaptation temperature interval of the bag type dust remover 2 can be just matched with the temperature of the flue gas at the outlet of the oil-fired boiler 1, and the smoke dust is captured through a plurality of filter bags in the bag type dust remover 2. The outlet of the ash bucket 21 is connected with a pneumatic ash conveying device, the pneumatic ash conveying device continuously sprays materials in the ash bucket 21 into a flue of the bag type dust collector 2, the phenomenon of oil smoke pasting is prevented, the materials in the ash bucket 21 adopt fly ash, viscous substances such as tar in the flue gas adhere to the surfaces of fly ash particles, and the viscous substances are blown into the ash bucket 21 along with a back blowing device 22 at the top of the bag type dust collector 2, so that the purposes of dust removal and oil removal are achieved. Since the bag filter 2 has high dust removal efficiency, the smoke concentration can be reduced to 10mg/Nm 3 The following is given.
Flue gas after dust removal treatment needs to enter a denitration unit, and medium-temperature SCR denitration technology is adopted for denitration to improve the adaptability of the system to sulfur in fuel oil. The flue gas temperature after dust removal is less than 200 ℃, so that the high-efficiency reaction temperature of the SCR denitration medium-temperature catalyst cannot be met. Thus, one innovation of the present application is that the flue gas is heated twice before it enters the SCR denitration reactor 5. In order to reduce the energy consumption of the system and comprehensively utilize the heat of the flue gas, the system is provided with a combined heating mode of the heat exchanger 3 and the hot blast stove 4 so as to improve the inlet temperature of the SCR denitration reactor 5. The heat exchanger 3 adopts a heat pipe type heat exchanger, a first air inlet of the heat exchanger is communicated with an air outlet of the bag type dust collector 2, and the heat exchanger is used for carrying out primary heating treatment on the flue gas subjected to dust removal treatment, and the primary heating is controlled at 200-270 ℃.
The fuel of the hot blast stove 4 adopts natural gas or diesel oil, the type is flue direct combustion type, and compared with a split hot blast stove system, the hot blast stove is simpler and more convenient to operate. The air inlet of the hot blast stove 4 is communicated with the first air outlet of the heat exchanger 3 and is used for carrying out secondary heating treatment on the flue gas subjected to primary heating, the secondary heating is controlled at 310-350 ℃, and the high-efficiency reaction temperature requirement of the medium-temperature catalyst of the SCR denitration reactor 5 is met. In this embodiment, the combustion load of the hot blast stove 4 is linked with the temperature value of the inlet of the SCR denitration reactor, the temperature control can be performed in a proportional adjustment mode according to the flow of the flue gas in the current flue, the adjustment ratio covers the load change range of the whole unit, and the load change of the system can be flexibly adapted.
In this embodiment, two layers of catalysts 51 are disposed inside the SCR denitration reactor 5, and the catalysts 51 may be honeycomb catalysts or plate catalysts, and in this embodiment, NO is formed after denitration treatment x The concentration can be reduced to 50mg/Nm 3 The following is given. In specific implementation, before the flue gas enters the SCR denitration reactor 5, a denitration reducing agent is injected into the flue, in this embodiment, ammonia water is injected by adopting the two-fluid spray gun 10, and after high-temperature gasification, the ammonia water is fully mixed with the flue gas and then enters the SCR denitration reactor 5 for flue gas denitration treatment.
Because the temperature of the flue gas at the outlet of the SCR denitration reactor 5 is higher, in the embodiment, the exhaust port of the SCR denitration reactor 5 is communicated with the second air inlet of the heat exchanger 4, and the flue gas after denitration is subjected to primary cooling treatment. In the actual production process, the temperature after the heat exchanger 4 is cooled still can be kept about 250 ℃, and at this time, if the flue gas is directly introduced into the desulfurization unit, unnecessary heat dissipation is caused. Another innovation of the system is therefore that a set of heat recovery units is provided before the flue gas is passed to the desulfurization unit. During implementation, the heat recovery unit adopts the finned tube heat exchanger 6, the air inlet of the finned tube heat exchanger 6 is communicated with the second air outlet of the heat exchanger 4, and is used for carrying out secondary cooling treatment on flue gas after denitration treatment, the secondary cooling is controlled at a temperature lower than 140 ℃, the temperature is higher than the acid dew point of the flue gas, the acid dew corrosion of downstream equipment is avoided, and meanwhile, the recovered flue gas heat can also be used for heating the water supply of the oil-fired boiler 1 or used as other heat supply sources, so that the utilization rate of waste heat resources is improved.
The system is flexibly provided with the heating and heat recovery units, and through reasonable combination of the heat exchanger 4, the hot blast stove 5 and the finned tube heat exchanger 6, the waste heat in the system is fully utilized, and the extra fuel consumption is reduced to the maximum extent. The heat recovered in the finned tube heat exchanger 7 is used for heating boiler feed water, the fuel consumption of the boiler is reduced by about 4 percent, and the comprehensive utilization of waste heat is realized.
In the system, the transmission resistance of the flue gas is overcome through the induced draft fan 7, the induced draft fan 7 is arranged between the finned tube heat exchanger 6 and the desulfurization unit, and because the position is a low-dust, low-temperature and low-corrosion area, the material selection of the induced draft fan 7 does not need to consider factors such as wear resistance, high temperature resistance, corrosion resistance and the like, the investment cost is low, and the service life of equipment is long. In specific implementation, the induced draft fan 7 can adopt a centrifugal fan, the pressure rise is 4000Pa-6000Pa, and a working mode of variable frequency adjustment is adopted. The rotation speed of the induced draft fan 7 is interlocked with the pressure value of the flue gas at the outlet of the boiler, the pressure of the flue gas is kept to be between 50Pa and 100Pa, and the induced draft fan 7 can flexibly adapt to the load change of a unit.
In this system, the desulfurization unit include with wet flue gas desulfurization absorption tower 8 of draught fan 7 gas vent intercommunication, can adopt wet flue gas desulfurization processes such as limestone-gypsum method, sea water method to carry out desulfurization treatment when specific implementation, be provided with the glass flake in the wet flue gas desulfurization absorption tower 8, have better anticorrosive effect, the top of the wet flue gas desulfurization absorption tower 8 sets up defroster 81, and defroster 81 adopts the polypropylene material to make for get rid of the droplet in the flue gas. Flue gas SO after desulfurization of the system 2 The concentration can be reduced to 35mg/Nm 3 And the method meets the standard requirements of ultra-low emission. Reference numeral 9 in fig. 2 denotes a chimney.
In addition, the embodiment embeds the smoke monitoring unit in the smoke discharging unit, SO that the smoke dust and SO in the smoke can be monitored in real time 2 、NO x And when the method is used for specific implementation, a plurality of groups of detection instruments can be arranged for detection, and data can be transmitted to the DCS automatic control system in real time, so that the monitoring is facilitated.
The application also provides a method for treating the ultralow emission of the tail gas of the oil-fired boiler based on the ultralow emission treatment system of the tail gas of the oil-fired boiler, which is shown in figure 3 and comprises the following steps:
s100, to be SO-containing 2 、NO x The method adopts fly ash to adsorb tar in the flue gas, and filters the flue gas by a filter bag in the bag type dust collector. Because the adaptive temperature interval of the bag type dust collector can be just matched with the temperature of the outlet smoke of the boiler, tar and smoke dust are collected through the filter bag of the bag type dust collector, and because the bag type dust collector has higher dust collection efficiency, the concentration of the smoke dust can be reduced to 10mg/Nm 3 The following is given.
S200, after the flue gas subjected to dust removal treatment is introduced into a heat exchanger and is primarily heated to 200-270 ℃, the flue gas is introduced into a hot blast stove and is secondarily heated to 310-350 ℃, the flue gas temperature is controlled to 310-350 ℃ through the two-time heating, the high-efficiency reaction temperature requirement of a medium-temperature catalyst of an SCR denitration reactor is met, an expensive low-temperature catalyst is not required to be equipped, only a small amount of necessary fuel and a cheap reducing agent are required, and the operation cost is low.
S300, ammonia water is injected into the flue gas subjected to the two-time heating treatment, the flue gas and the ammonia water subjected to the high-temperature gasification are uniformly mixed, then the flue gas is introduced into an SCR denitration reactor, denitration reaction is carried out under the action of a medium-temperature denitration catalyst, and NO is obtained x Is converted into N 2 And H 2 O. In specific implementation, two layers of catalysts are arranged in the denitration reactor, the catalysts are honeycomb type or plate type, and NO is obtained after denitration treatment x The concentration can be reduced to 50mg/Nm 3 The following is given.
S400, the flue gas after denitration and purification is led into the heat exchanger again for primary cooling, the temperature is reduced to 240-280 ℃, and then the flue gas is led into the finned tube heat exchanger for heat recovery, so that the flue gas is cooled to less than 140 ℃ for the second time.
S500, introducing the flue gas subjected to the twice cooling treatment into a wet desulfurization absorption tower for desulfurization treatment. In the concrete treatment, a limestone-gypsum method, a seawater method and other wet desulfurization processes are adopted for desulfurization treatment.
S600, the purified flue gas is discharged after being monitored.
In the present specification, each embodiment is described in a progressive manner, and each embodiment is mainly described in a different point from other embodiments, and identical and similar parts between the embodiments are all enough to refer to each other. For the system disclosed in the embodiment, since it corresponds to the method disclosed in the embodiment, the description is relatively simple, and the relevant points refer to the description of the method section.
The principles and embodiments of the present application have been described herein with reference to specific examples, the description of which is intended only to assist in understanding the methods of the present application and the core ideas thereof; also, it is within the scope of the present application to be modified by those of ordinary skill in the art in light of the present teachings. In view of the foregoing, this description should not be construed as limiting the application.

Claims (8)

1. The system is characterized by further comprising a dust removal unit, a heating unit, a denitration unit, a heat recovery unit, an induced draft fan, a desulfurization unit and a flue gas discharge unit which are sequentially communicated through pipelines;
the dust removing unit is used for collecting raw flue gas exhausted by the oil-fired boiler and carrying out dust removing treatment operation on the raw flue gas so as to reduce the concentration of smoke dust to 10mg/Nm 3 The following are set forth;
the heating unit comprises a heat exchanger and a hot blast stove which are sequentially connected; the heat exchanger is used for carrying out primary heating treatment on the clean flue gas subjected to dust removal treatment, and the primary heating is controlled at 200-270 ℃; the hot blast stove is used for carrying out secondary heating treatment on the clean flue gas subjected to primary heating, and the secondary heating is controlled at 310-350 ℃;
the denitration unit comprises a reducing agent injection device connected with a flue of the hot blast stove and an SCR denitration reactor connected with the tail end of the flue of the hot blast stove, and the denitration adopts a medium-temperature SCR denitration technology; the reducing agent injection device adopts a double-fluid spray gun to inject ammonia water, the ammonia water is gasified at high temperature and then fully mixed with the flue gas, and the mixture enters the SCR denitration reactor to be subjected to flue gas denitration treatment, so that NO x The concentration is reduced to 50mg/Nm 3 The following are set forth; the exhaust port of the SCR denitration reactor is communicated with the second air inlet of the heat exchanger, and the flue gas subjected to denitration treatment is subjected to primary cooling treatment;
the heat recovery unit is used for cooling and recovering heat of the flue gas subjected to denitration treatment; the heat recovery unit comprises a finned tube heat exchanger; the fin tube heat exchanger is used for carrying out secondary cooling treatment on the flue gas subjected to denitration treatment, and the secondary cooling is controlled in a range that the temperature is lower than 140 ℃ and is higher than the acid dew point of the flue gas; the heat recovered by the finned tube heat exchanger is used for heating fuel oil and water supply;
the induced draft fan is used for providing power for transmitting the smoke in the pipeline and controlling the smoke pressure value in the system;
the desulfurization unit is used for acquiring the flue gas transmitted by the induced draft fan and carrying out desulfurization treatment operation on the flue gas SO as to enable SO (sulfur-doped oxygen) 2 The concentration is reduced to 35mg/Nm 3 The following are set forth; the desulfurization unit comprises a wet desulfurization absorption tower communicated with an exhaust port of the induced draft fan;
the flue gas discharge unit is used for discharging the flue gas treated by the system outwards; the flue gas exhaust unit is internally provided with a flue gas monitoring unit which is used for detecting whether the content of pollutants in the flue gas accords with the emission standard or not and monitoring the smoke dust and SO in the flue gas in real time 2 、NO x Is transmitted to the DCS automatic control in real timeA unit.
2. The ultra-low emission treatment system of an oil-fired boiler tail gas according to claim 1, wherein the dust removal unit comprises a bag filter; the outlet of the ash bucket of the bag type dust collector is connected with a pneumatic ash conveying device, and fly ash in the ash bucket is sprayed into a flue of the bag type dust collector and used for adsorbing tar in the fed raw flue gas; a plurality of filter bags are uniformly distributed in the bag type dust collector and are used for filtering smoke dust, and a back blowing device is arranged at the top of the bag type dust collector and is used for blowing the smoke dust and the coal ash adsorbed with tar into an ash bucket at regular time; the clean flue gas is exhausted through an exhaust port located at the top of the bag house.
3. The ultra-low emission treatment system of tail gas of an oil-fired boiler according to claim 1, wherein the heat exchanger adopts a heat pipe type, and a first air inlet of the heat exchanger is communicated with an air outlet of the bag filter;
the hot blast stove adopts a flue direct combustion type, and an air inlet of the hot blast stove is communicated with a first air outlet of the heat exchanger.
4. The ultra-low emission treatment system of an oil-fired boiler tail gas according to claim 1, wherein an exhaust port of the SCR denitration reactor is communicated with a second air inlet of the heat exchanger;
the air inlet of the finned tube heat exchanger is communicated with the second air outlet of the heat exchanger.
5. The ultralow emission treatment system for the tail gas of the oil-fired boiler according to claim 1, wherein two layers of catalysts are arranged in the SCR denitration reactor up and down, and the catalysts are honeycomb type or plate type catalysts.
6. The ultra-low emission treatment system of tail gas of a fuel oil boiler according to claim 1, wherein the induced draft fan adopts a variable frequency centrifugal fan.
7. The ultralow emission treatment system for the tail gas of the oil-fired boiler according to claim 1, wherein glass flakes are arranged in the wet desulfurization absorption tower, and a demister is arranged at the top of the wet desulfurization absorption tower to remove fog drops in flue gas.
8. An ultralow emission treatment method for tail gas of a fuel oil boiler, which is characterized by adopting the ultralow emission treatment system for tail gas of a fuel oil boiler as claimed in any one of claims 1-7 for treatment, comprising the following steps:
will contain SO 2 、NO x And the flue gas of the oil-fired boiler with the smoke dust is introduced into a bag type dust collector for dust removal treatment, so that the concentration of the smoke dust is reduced to 10mg/Nm 3 The following are set forth;
introducing the clean flue gas subjected to dust removal treatment into a heat exchanger, primarily heating to 200-270 ℃, and then introducing into a hot blast stove to secondarily heat to 310-350 ℃;
ammonia water is injected into the flue gas after the two heating treatments, the flue gas and the ammonia water after the high temperature gasification are evenly mixed, then the flue gas is introduced into an SCR denitration reactor, denitration reaction is carried out under the action of a medium temperature denitration catalyst, and NO is obtained x Conversion to N 2 And H 2 O, so that NO x The concentration is reduced to 50mg/Nm 3 The following are set forth;
the flue gas after denitration and purification is led into a heat exchanger again for primary cooling, the temperature is reduced to 240-280 ℃, and then is led into a finned tube heat exchanger for heat recovery, so that the flue gas is secondarily cooled to less than 140 ℃;
the flue gas subjected to the twice cooling treatment is led into a wet desulfurization absorption tower for desulfurization treatment, SO that SO 2 The concentration is reduced to 35mg/Nm 3 The following are set forth;
and the purified flue gas is discharged after flue gas detection.
CN202310850341.7A 2022-05-30 2022-05-30 Ultralow emission treatment system and method for tail gas of oil-fired boiler Pending CN116764377A (en)

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