CN112569758B - Online denitration process for sintering flue gas - Google Patents
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Abstract
The invention relates to an online denitration process for sintering flue gas, which adopts the technical scheme that sintering airflow enters a sintering material layer to support combustion and sinter to form sintering flue gas under the suction action of a fan, and the sintering flue gas passes through the sintering material layer, a sintering machine trolley grate and an air box and enters a main flue; dividing the sintering machine into an ignition region, a low-temperature flue gas region, a flue gas rapid heating region, a NOx concentration rapid reduction region and a high-temperature flue gas region in sequence along the traveling direction of a trolley; the sintering flue gas is collected through a low-temperature flue gas main flue, a high-NOx flue gas main flue and a high-temperature flue gas main flue respectively, the sintering flue gas of the low-temperature flue gas main flue is mixed with ammonia gas, the mixture is introduced into a low-temperature flue gas circulating cover above a sintering material layer in a high-temperature flue gas area through a low-temperature flue gas pipeline and enters the sintering material layer again, the temperature in the sintering material layer is raised, and reduction denitration is carried out under the catalytic action of iron-based polyoxide rich in the sintering material layer. The invention has simple process, small occupied area and low operation cost, and does not need an externally purchased denitration catalyst.
Description
Technical Field
The invention relates to an industrial flue gas purification process in the field of environmental protection, in particular to an online denitration process for sintering flue gas.
Background
Since the 21 st century, with the improvement of emission standards in the steel industry, various steel enterprises have been continuously matched with desulfurization processes for flue gas of sintering machines, and in 2016, all existing sintering machines have been basically matched with desulfurization devices. In recent years, with the strictness of emission standards, denitration facilities are constructed in cooperation with steel mills. Because steel mills are built with desulfurization facilities for sintering flue gas in the earlier stage, 3 schemes of 'synchronous denitration by a matched wet desulfurization process', 'series connection of independent denitration devices' and 'new construction of integrated desulfurization and denitration devices for sintering flue gas' are generally adopted when matched denitration facilities are adopted.
The first scheme is that strong oxidant, such as ozone, hydrogen peroxide, etc. is sprayed into the flue with wet desulfurizing process to oxidize NOx into high valence NOx, and the NOx is absorbed in desulfurizing tower and exhausted via waste water.
Principle of reaction NO + strong oxidant → NO 2 +NO 3 +N 2 O 5
The process route transfers the gaseous nitrogen oxide into the wastewater, so that the nitrogen content in the wastewater is increased, and the nitrogen-containing wastewater is difficult to treat; in addition, the process consumes much power and produces ozone pollution. Therefore, the method is not suitable for treating the nitrogen oxides with large smoke volume of the sintering machine.
The second scheme is that a denitration device is added after the existing wet or semi-dry desulfurization device. At present, a selective catalytic reduction denitration (SCR) process is basically adopted by a denitration device additionally arranged in domestic steel plants, a low-temperature catalyst is used in the technology, the flue gas is heated to 240 ━ 280 ℃ by using coal gas, then ammonia gas is sprayed in, and NOx generates nitrogen and water under the action of the catalyst.
Reaction principle (under the catalysis of catalyst) NO + NO 2 +NH 3 →N 2 +H 2 O
The process route has high denitration efficiency, the process is mature, but the energy consumption is high, one layer of catalyst needs to be replaced every three years, and the replaced catalyst belongs to dangerous waste and is difficult to treat.
The desulfurization and denitrification technology of the sintering flue gas in the third scheme can be mainly divided into a dry method and a wet method.
1. Dry flue gas desulfurization and denitration technology
The dry desulfurization and denitrification refers to a desulfurization process in which the added desulfurization and denitrification absorbent and desulfurization and denitrification products are dry, and is characterized in that the solid absorbent removes SO in a dry state 2 And NO, and the absorbent is treated or regenerated in a dry state, without waste liquid, but with a low removal efficiency.
(1) Pulse corona method
The pulse corona desulfurization and denitrification technology utilizes the generated high-energy electrons to impact background gas to generate a large amount of free radicals to SO 2 And NO to generate SO respectively 3 And NO 2 Or the corresponding acid, in the presence of an additive such as ammonia, the resulting ammonium salt settles out and can be used as a fertilizer. The plasma method has the advantages of simple process flow, less investment compared with a wet method, higher desulfurization and denitrification rate, and utilization of byproducts, but also has the disadvantages of high power consumption and secondary pollution caused by ammonia emission.
(2) Electron beam irradiation method
The electron beam irradiation desulfurization and denitration technology is a desulfurization and denitration technology combining physical and chemical principles. It uses electron accelerator to generate active substances with strong oxidizing property, such as free radical, etc. to remove NO and SO in flue gas 2 Oxidation to NO 2 And SO 3 These high-priced nitrogen oxides and sulfur oxides react with water vapor to form atomized nitric acid and sulfuric acid, and react with the added NH 3 The ammonium nitrate and the ammonium sulfate are generated by reaction, and the aims of denitration and desulfurization are fulfilled. The electron beam irradiation method has high efficiency of simultaneously removing sulfur and nitrogen; the byproducts ammonium sulfate and ammonium nitrate can be used as fertilizer; the system is simple, the operation is convenient, and the process is easy to control; for different contentsThe flue gas with the sulfur content and the change of the flue gas content have better adaptability and load tracking property. However, the method has high power consumption and high operating cost; the flue gas radiation device is limited to be used in large-scale application systems; the treated flue gas still has the possibility of discharging secondary pollution
(3)CuO/γ-Al 2 O 3 Catalytic absorption process
CuO/gamma-Al in catalyst for dry catalysis and simultaneous desulfurization and denitrification 2 O 3 Can adsorb SO in flue gas at 300-450 DEG C 2 Catalytically oxidizing it to sulfate, and CuSO 4 CuO has high catalytic activity for reducing NOx by a Selective Catalytic Reduction (SCR) method, and can simultaneously reduce NOx in flue gas into N by Selective Catalytic Reduction (SCR) under the condition of ammonia injection 2 。
(4) Adsorption method with activated carbon
The method utilizes active coke to simultaneously desulfurize and denitrate flue gas. SO (SO) 2 The sulfuric acid is removed by microporous catalytic adsorption of active coke, the generated sulfuric acid is stored in micropores of the coke, and then the sulfuric acid is regenerated by heat. The NOx is removed by adding ammonia, and water and nitrogen are generated through the catalytic action of active coke and then discharged into the atmosphere. The following problems exist in the application of the activated carbon/activated coke desulfurization and denitrification process:
firstly, the operation of the chain bucket machine home-made equipment is unstable, and the breakage rate of the active carbon/active coke is easily increased, so that the chain bucket equipment of a large sintering machine needs to adopt equipment of Japanese brand, the price of the part of equipment is higher, and the chain bucket machine needs to be localized as soon as possible so as to reduce the investment cost of the whole set of equipment.
Secondly, the operation temperature of the hot air circulating fan in the desorption system is up to 500-600 ℃, and the type selection of the equipment needs to be paid attention to.
And thirdly, the temperature of the active carbon/active coke in the adsorption tower needs to be paid special attention during operation, so that hot spots and even fire phenomena are prevented.
(5) Other dry desulfurization and denitrification technologies
In recent years, the dry flue gas desulfurization and denitration technology is continuously developed and improved, and also comprises a plurality of other technologies: an electrocatalytic oxidation method (ECO), an NH/VO-TiO method, an NOxSO method, a Pahlman flue gas desulfurization and denitrification process, an organic calcium salt desulfurization and denitrification technology and the like.
2. Wet desulfurization and denitrification technology
The wet flue gas desulfurization and denitration technology means that the desulfurization and denitration agent and the desulfurization and denitration product are in a wet state. At present, the flue gas denitration absorption reaction can be mainly divided into three types, namely oxidation absorption, complexation absorption and reduction absorption according to different treatment modes of NO.
(1) Oxidative absorption process
NO is not absorbed either in water or in lye, except for the formation of complexes. It is necessary to oxidize part of NO to NO 2 Then absorbed and removed by alkali liquor. The strong oxidant which is researched more at present is NaClO 2 、H 2 O 2 、KMnO 4 、O 3 。
(2) Complex absorption method
In the complex absorption, a liquid-phase complex is added into a liquid-phase denitration solvent and can perform a rapid complex reaction with NO, so that the solubility of NO is increased, the aim of denitration is fulfilled, and a cobalt complex and a ferrous complex are researched more.
(3) Reduction absorption method
Reductive adsorption refers to the reduction of NOx to N in the liquid phase 2 The absorption process of (1). Most studied so far are urea and ammonium sulfite.
At present, most steel mills select an activated carbon/activated coke process when a sintering flue gas desulfurization and denitrification device is newly built, but the process has the following problems in the operation process:
firstly, the operation of the chain bucket machine home-made equipment is unstable, and the breakage rate of the active carbon/active coke is easily increased, so that the chain bucket equipment of a large sintering machine needs to adopt equipment of Japanese brand, the price of the part of equipment is higher, and the chain bucket machine needs to be localized as soon as possible so as to reduce the investment cost of the whole set of equipment.
The operation temperature of a hot air circulating fan in the desorption system is up to 500-600 ℃, and the type selection of equipment needs attention.
And thirdly, the temperature of the active carbon/active coke in the adsorption tower needs to be paid special attention during operation, so that hot spots and even fire phenomena are prevented.
Meanwhile, the process has large investment, in order to improve the denitration efficiency, the investment of the activated carbon/activated coke which is only initially loaded accounts for more than 30 percent of the total investment, the operation cost is also higher, and the process is generally applied to 18 yuan/t-sinter ore in steel mills.
Although the selective catalytic reduction denitration (SCR) process is mature and stable in operation, extra heat energy needs to be supplemented when SCR catalytic reduction denitration is carried out due to the fact that the sintering flue gas temperature is low, and the operation cost of SCR denitration is additionally increased. Meanwhile, the key of SCR catalytic reduction denitration is a denitration catalyst, and in the total investment of an SCR denitration system, the investment cost of the catalyst accounts for more than 30%, so that the development of a novel cheap and efficient denitration catalyst is the general trend of the research on the SCR denitration technology of domestic and foreign flue gas.
Pio et al have studied noble metal catalysts and have studied treatment and modification of noble metal catalysts to obtain noble metal catalysts with better catalytic activity, stronger thermal stability and longer service life, but noble metals are expensive, resulting in increased catalyst cost. Therefore, in recent years, researchers have been studying to replace relatively inexpensive metal oxides.
In the steel industry, metal oxides, particularly iron-based polyoxides, generally exist in the whole process of steel production, and if the iron-based polyoxide can be used as a flue gas denitration catalyst, the denitration cost can be greatly reduced. Based on the thought, the technology removes the NOx in the flue gas by utilizing the characteristic that the sinter is rich in iron-based polyoxide.
Disclosure of Invention
Aiming at the problems of large investment, high operation cost, difficult treatment of waste catalyst and the like of the existing sintering flue gas denitration process, the invention provides the sintering flue gas on-line denitration process which has the advantages of simple system, no catalyst purchase, energy conservation, consumption reduction, small occupied area and low investment and operation cost of flue gas denitration equipment.
The process comprises the steps that sintering airflow enters a sinter bed to support combustion and sinter to form sintering flue gas under the suction action of a fan, and the sintering flue gas passes through the sinter bed, a sintering machine trolley grate and an air box below a trolley and enters a main flue; the sintering machine is divided into an ignition area, a low-temperature smoke area, a smoke rapid heating area, a NOx concentration rapid reducing area and a high-temperature smoke area 5 areas in sequence along the travelling direction of a sintering machine trolley; the ignition area accounts for 2-3 bellows, the low-temperature flue gas area accounts for 50-55% of the total length of the sintering machine, the flue gas rapid heating area accounts for 10-15% of the total length of the sintering machine, the NOx concentration rapid reduction area accounts for 10-15% of the total length of the sintering machine, and the high-temperature flue gas area accounts for 15-20% of the total length of the sintering machine, wherein the sintering flue gas is collected through 3 main flues including a low-temperature flue gas main flue, a high-NOx flue gas main flue and a high-temperature flue gas main flue; the low-temperature flue gas main flue correspondingly collects sintering flue gas in an ignition region and a low-temperature flue gas region, the high-NOx flue gas main flue correspondingly collects sintering flue gas in a flue gas rapid heating region and a NOx concentration rapid reducing region, and the high-temperature flue gas main flue correspondingly collects sintering flue gas in a high-temperature flue gas region; 2-4 groups of air box smoke outlets of the low-temperature smoke area, which are close to the smoke rapid heating area, are respectively connected with a low-temperature smoke main flue and a high NOx smoke main flue through exchange valves; 2-4 groups of air box smoke outlets adjacent to the high-temperature smoke area and the NOx concentration rapid reduction area are respectively connected with a high-NOx smoke main flue and a high-temperature smoke main flue through exchange valves; the sintering flue gas collected by the low-temperature flue gas main flue is mixed with ammonia gas, the mixture is introduced into a low-temperature flue gas circulating cover above a sintering material layer in a high-temperature flue gas area through a low-temperature flue gas pipeline, the mixture enters the sintering material layer again under the suction action of a fan, the temperature of the mixture is raised in the sintering material layer, and NOx in the sintering flue gas and the ammonia are subjected to reduction denitration reaction under the catalytic action of iron-based polyoxide contained in the sintering material layer. At least 1 layer of ammonia water or liquid ammonia nozzles are circumferentially arranged on the side wall of the low-temperature flue gas pipeline, the nozzles eject ammonia water or liquid ammonia, and the molar ratio of the ammonia-containing amount of the ejected ammonia water or liquid ammonia to the NOx content in the sintering flue gas is 0.8-0.9; and the ammonia water or the liquid ammonia is gasified into ammonia gas in the sintering flue gas and enters the ammonia gas mixer together with the sintering flue gas to be mixed, and the sintering flue gas and the ammonia gas are mixed and then enter the low-temperature flue gas circulation cover above the sintering material layer in the high-temperature flue gas area.
And introducing the sintering flue gas of the low-temperature flue gas main flue into a low-temperature flue gas circulation cover above a sintering material layer in a high-temperature flue gas area through a low-temperature flue gas pipeline after introducing the sintering flue gas into an ammonia desulphurization system for desulphurization.
And improving the depth of ammonia water of the desulfurization absorbent of the ammonia desulfurization system to improve the ammonia escape amount, and controlling the molar ratio of the ammonia escape amount to the NOx content in the sintering flue gas to be 0.8-0.9.
And increasing the length of the high-temperature flue gas area and shortening the length of the low-temperature flue gas area by adjusting the thickness of the sintering material layer or the advancing speed of a sintering machine trolley.
By reducing the thickness of the sintering material layer by 5-10 percent or reducing the traveling speed of the sintering machine trolley by 5-10 percent.
The length of the high-temperature flue gas area is increased to 40-45% of the total length of the sintering machine, the length of the low-temperature flue gas area is shortened to 38-43% of the total length of the sintering machine, the rapid flue gas temperature rising area accounts for 5-10% of the total length of the sintering machine, and the rapid NOx concentration reduction area accounts for 5-10% of the total length of the sintering machine.
And the sintering flue gas from the high-NOx flue gas main flue is conveyed into the high-NOx flue gas circulation cover above the sintering material layer in the low-temperature flue gas area through the high-NOx flue gas pipeline, and enters the sintering material layer again for recycling under the suction action of the fan.
And supplementing oxygen to the flue gas in the high NOx flue gas main flue, mixing the oxygen by an oxygen mixer, and then entering the high NOx flue gas circulating cover.
The low-temperature flue gas circulation cover and the high NOx flue gas circulation cover are uniformly distributed with a plurality of airflow balance pipes, the airflow balance pipes are provided with one-way flap valves, and air passes through the balance pipes and penetrates through the flap valves from top to bottom to enter a sinter bed.
And sintering flue gas from the high-temperature flue gas main flue enters a flue gas desulfurization system after dust removal and waste heat recovery.
The high NOx flue gas circulation cover covers the low-temperature flue gas area and a part of flue gas rapid temperature rising area close to the low-temperature flue gas area.
The low-temperature flue gas circulating cover covers the high-temperature flue gas area and a part of NOx concentration rapid reduction area close to the high-temperature flue gas area.
The trolley and the sintering mixture run from the head to the tail in an inclined upward manner, and the sintering airflow and the sintering flame frontal surface are perpendicular to the travelling direction of the trolley and obliquely pass through the sintering material layer downwards.
The trolley and the sintering mixture on the trolley run from the head to the tail in an inclined mode, and the inclination is 5-15%.
A plurality of temperature monitors are arranged on the inner sides of the edges of the high-NOx smoke circulating cover and the low-temperature smoke circulating cover, and monitoring signals are interlocked with the high-NOx smoke circulating fan and the low-temperature smoke exhaust fan.
And when the temperature monitor monitors that the temperature of the airflow is higher than the room temperature, the air box flue gas outlet exchange valves of the two main flues are switched and connected, and the sintering flue gas amount entering the flue gas main flue is adjusted.
And when the temperature monitor monitors that the temperature of the airflow is higher than the room temperature, adjusting the air suction volume of a fan connected with the corresponding flue gas main flue.
The inventor researches and discovers that the concentration of NOx in the sintering flue gas generated in the ignition region and the low-temperature flue gas region is higher in 5 regions of the sintering machine, and the concentration is generally 400mg/m 3 The above; the concentration of NOx contained in the flue gas generated in the rapid heating area of the flue gas begins to decrease, but the decrease trend is not large; the concentration of NOx contained in the smoke generated in the NOx concentration rapid reduction area is rapidly reduced from 300mg/m 3 Quickly decreases to 50mg/m 3 The following; the concentration of NOx in the flue gas generated in the high-temperature flue gas area is lower than 50mg/m 3 。
Aiming at the problems in the background art, the inventor makes the following improvements by combining the characteristics of different sintering flue gas properties of different regions of a sintering machine: using iron-based polyoxides, e.g. gamma-Fe, enriched in sinter 2 O 3 To NH 3 And SCR denitration has the characteristic of stronger catalytic activity, sintering flue gas is collected in a partition mode and circulated in a quality-divided mode, one part of the flue gas containing high NOx concentration in a low-temperature flue gas area is collected and enters a low-temperature flue gas main flue, and the other part of the flue gas containing high NOx concentration enters a high-NOx flue gas main flue. Mixing the flue gas entering the low-temperature flue gas main flue and ammonia gas generated after volatilization of liquid ammonia or ammonia water sprayed into the flue gas pipeline by an ammonia gas mixer, introducing the mixture to the upper part of a sinter bed in a flue gas rapid temperature rise region and a NOx concentration rapid reduction region of a sintering machine,under the suction action of fans in the smoke rapid temperature rising area and the NOx concentration rapid reduction area, smoke enters the sinter bed again, the temperature rises in the sinter bed, the smoke mixed with ammonia gas rises to reach the reaction temperature of SCR and SNCR, and NOx reduction denitration reaction is carried out under the catalytic action of the sinter bed.
In order to ensure the smooth circulation of the flue gas and the balance of the flue gas amount and further reduce the amount of discharged sintering flue gas, a part of the flue gas with high NOx concentration generated in a low-temperature flue gas area is collected and enters a high-NOx flue gas main flue, is mixed with the sintering flue gas collected by the main flue and coming from a flue gas rapid temperature raising area and a NOx concentration rapid reducing area, and simultaneously, supplemented oxygen is recycled and enters a high-NOx flue gas circulation cover above the low-temperature flue gas area, and enters a sintering material layer for recycling under the suction effect of a fan, and NOx is enriched.
Further research shows that in the NOx concentration rapid reduction area and the high-temperature flue gas area, fuel in the sintering material layer is completely combusted, the sintering material layer is completely formed into a sintering ore layer, and the sintering ore layer is high in porosity, large in pore diameter and small in gas resistance. When the circulating flue gas enters the sinter bed, the circulating flue gas exchanges heat with the sinter to raise the temperature, and simultaneously NOx in the flue gas and the sprayed ammonia can perform reduction denitration reaction under the catalytic action of iron-based polyoxide rich in the sinter bed.
According to analysis on the principle of belt type air draft sintering, after the sintering material is ignited at high temperature, the fuel in the sintering material layer is continuously combusted to form a combustion layer. The flame front moves downwards continuously along with the proceeding of air draft sintering. The fuel in the sinter material is burnt to release a large amount of heat, so that the minerals in the material layer are melted, and the generated molten liquid phase is cooled and recrystallized (1000-1100 ℃) to be solidified into the sinter with a mesh structure, namely the sinter layer, along with the downward movement of the burning layer and the passing of cold air. The main change in this layer is solidification of the melt, with crystallization and precipitation of new minerals. As sintering proceeds, the gas stream is preheated through the sinter bed while the sinter is cooled and the suboxides may be reoxidized upon contact with air.
Because the combustion air of the combustion layer is preheated by the sintering ore layer, the temperature of the layer is high, and the temperature of the flame front reaches 1350-1600 ℃, so that the minerals are softened, melted and bonded into blocks. In addition to the combustion reaction, the layer also undergoes reactions such as melting, reduction, oxidation of solid materials, and decomposition of limestone and sulfides.
When high-temperature flue gas generated after fuel in the combustion layer is combusted downwards passes through the sinter layer, the mixture at the lower part is quickly preheated to the ignition temperature, generally 400-800 ℃, and then the preheating layer is formed. Solid phase reaction begins in the layer, crystal water and partial carbonate and sulfate are decomposed, and magnetite is partially oxidized.
The flue gas passing through the preheating layer continuously downwards passes through the sintering material layer, and the lower layer of sintering mixture is quickly dried to form a drying layer. The temperature of the layer rises to above 100 ℃ quickly, a large amount of free water in the mixture evaporates, and the thickness of the layer is l 0-30 mm generally.
In actual production, the drying layer is difficult to separate from the preheating layer, and is generally referred to as a dry preheating layer. The material balls in the layer are rapidly heated, rapidly dried and easily damaged, and the air permeability of the material layer is deteriorated.
The hot waste gas from the drying layer contains a large amount of moisture, and when the material temperature is lower than the dew point temperature of the water vapor, the water vapor in the waste gas can be condensed again, so that the moisture in the mixed material is increased greatly to form an over-wet layer. The moisture in the layer is too much, so that the air permeability of the material layer is deteriorated, and the sintering speed is reduced.
When the flue gas passing through the over-wet layer downwards passes through the sintering mixture, the flue gas is continuously cooled by the material layer, the temperature of the flue gas leaving the sintering mixture layer is about 80 ℃, and the humidity is in a relative saturation state.
After entering the bellows, influenced by ambient temperature, the temperature can further reduce, and the flue gas is in humidity oversaturation state. At this time, the ammonia water is sprayed into the flue gas, the temperature of the flue gas is reduced again under the influence of the temperature of the ammonia water and the volatilization and heat absorption of the ammonia water, and the humidity is further increased. The temperature of the flue gas is 70-80 ℃. The temperature and humidity environment is very favorable for the reaction of sulfur dioxide in the flue gas and ammonia gas, and the flue gas is introduced into a wet ammonia desulphurization system or a desulphurization system of other process technologies, so that the desulphurization efficiency is high. Aiming at a wet ammonia desulfurization system, certain ammonia escape amount of desulfurized flue gas is kept so as to improve desulfurization efficiency, and an ammonia source is provided for subsequent flue gas denitration. The mol ratio of the escape amount of ammonia to the NOx content in the sintering flue gas is controlled to be 0.8-0.9.
In order to reduce the amount of discharged sintering flue gas and ensure the denitration effect of a high-temperature flue gas region, the operation process parameters of the sintering machine are adjusted, such as the thickness of a sintering material layer is reduced or the travelling speed of a trolley of the sintering machine is reduced. The length of the high-temperature flue gas area is adjusted to be increased to 40-45% of the total length of the sintering machine, and the length of the low-temperature flue gas area is shortened to reach 38-43% of the total length of the sintering machine, so that sintering flue gas collected by the low-temperature flue gas main flue can completely enter the high-temperature flue gas area.
The inventor further researches and discovers that as the flue gas circulation is carried out, in a low-temperature flue gas area, the temperature and the humidity of sintering flue gas are basically kept unchanged, but the concentration of sulfur dioxide in the flue gas is obviously increased and is kept at 3000mg/m of 2000- 3 In order to improve the on-line denitration effect, the flue gas is firstly led out for desulfurization and then returned to the low-temperature flue gas circulation cover to enter the sinter bed for denitration.
Has the advantages that:
(1) need not newly-built sintering flue gas denitration facility, save denitration equipment input and denitration running cost. By utilizing the characteristics of higher temperature of a sintering ore layer, high porosity, large pore diameter and small gas resistance of a high-temperature flue gas area at the tail part of the sintering machine, sintering flue gas containing higher concentration of NOx in a head part area of the sintering machine circularly enters the sintering ore layer at the tail part area of the sintering machine to participate in sintering again. Under the heat exchange action of the sintered ore layer, the temperature is raised, and under the catalytic action of iron-based polyoxide rich in the sintered ore layer, NOx in the flue gas and the injected ammonia can perform reduction denitration reaction. And an external denitration catalyst is not needed, the investment of denitration equipment is not needed, and the investment and running cost of denitration are greatly reduced.
(2) The smoke discharge is reduced by more than 60 percent. Through the circulation of the sintering flue gas in different qualities and regions, the emission of the flue gas is greatly reduced, the concentration of pollutants in the flue gas is enriched, and the removal effect of the pollutants is improved.
(3) The flue gas circulation operation stability is high, and the flue gas volume balancing capability is strong. Part of the flue gas with high concentration of NOx generated in the low-temperature flue gas area is collected and enters a high-NOx flue gas main flue, and is mixed with the sintering flue gas collected by the main flue and coming from the flue gas rapid temperature rising area and the NOx concentration rapid reduction area, and meanwhile, the supplementary oxygen is recycled and enters a high-NOx flue gas recycling cover above the low-temperature flue gas area, and enters a sintering material layer again for recycling under the suction effect of a fan. The oxygen content of the circulating flue gas can be balanced by supplementing oxygen; a part of smoke in the low-temperature smoke area enters the high-NOx smoke main flue to form a part of internal circulation path, so that the improvement of the stability of smoke circulation and the balance of smoke quantity are facilitated.
(4) The problem of ammonia escape in the prior ammonia desulphurization of the sintering flue gas is solved. The residual ammonia in the flue gas is just used as a reducing agent for denitration, so that the problem of ammonia escape which is difficult to overcome in the ammonia desulphurization of the sintering flue gas is solved, and the ammonia resource is fully utilized.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Fig. 2 is a drawing of embodiment 2 of the present invention.
Wherein, 1-sintering machine, 1.1-trolley, 2-sinter bed, 2.1-sinter mixture, 2.2-bedding material, 3-1-low temperature smoke circulating cover, 3-2-high NOx smoke circulating cover, 4-1-low temperature cover air inlet balance pipe, 4-2-high NOx cover air inlet balance pipe, 5-1-low temperature cover air inlet balance valve, 5-2-high NOx cover air inlet balance valve, 6-1-low temperature smoke pipeline, 6-2-high NOx smoke pipeline, 6-3-high temperature smoke pipeline, 7-ignition system, 8-blanking chute, 9-material distribution system, 9.1-blanking hopper, 9.2-material distributor, 10-head traction mechanism, 10.1-head star wheel, 11-1-ammonia mixer, 11-2-oxygen mixer, 12-air box, 13-tail traction mechanism, 13.1-tail star wheel, 2-sinter bed, 2.1-sinter bed, 2-sinter mixture, 2-sinter bed, 3-high NOx cover air inlet balance pipe, 5-1-low temperature smoke pipe, 6-3-high NOx cover air inlet balance pipe, 9-1-high NOx cover air inlet balance valve, 9-high NOx cover air inlet balance pipe, 9-material distribution system, 9.1-discharge system, 9.2-discharge system, 10-head star wheel, 2-pallet, and-pallet, 2-pallet, and the like, 14.1-ammonia water nozzle, 14.2-ammonia water mist, 15-desulfurization system, 16-1-high temperature flue gas main flue, 16-2-high NOx flue gas main flue, 16-3-low temperature flue gas main flue, 17-exchange valve, 18-1-high temperature flue gas dust remover, 18-2-high NOx flue gas dust remover, 18-3-low temperature flue gas dust remover, 19-waste heat boiler, 20-external exhaust flue gas dust remover, 21-1-external exhaust flue gas fan, 21-2-high NOx flue gas fan, 21-3-desulfurization flue gas fan, 21-4-low temperature flue gas fan and 22-desulfurization flue gas dust remover.
Detailed Description
The invention is further explained by means of embodiments in connection with the attached drawings.
Example 1
See FIG. 1, 450m from a certain Steel works 2 The sintering machine of (1) has 24 groups (48) of windboxes 12 in total. Sintering airflow passes through a sintering material layer 2, a bedding material 2.1, a trolley 1.1 grate of a sintering machine 1 and an air box 12 below the trolley 1.1 to enter a main flue (comprising a high-temperature flue gas main flue 16-1, a high-NOx flue gas main flue 16-2 and a low-temperature flue gas main flue 16-3) under the suction action of a fan (comprising an outward-discharging flue gas fan 21-1, a high-NOx flue gas fan 21-2, a desulfurization flue gas fan 21-3 and a low-temperature flue gas fan 21-4); the sintering machine is divided into an ignition area, a low-temperature flue gas area, a flue gas rapid heating area, a NOx concentration rapid reduction area and 5 high-temperature flue gas areas in sequence along the traveling direction of a trolley 1.1 of the sintering machine 1. The sintering mixture is uniformly distributed on a trolley 1.1 of the sintering machine 1 through a discharging chute 8 by a discharging hopper 9.1 and a distributing machine 9.1. Under the pushing of the rear trolley 1.1, the trolley 1.1 loaded with the sinter bed 2 moves to the lower part of the ignition system 7 and ignites and sinters, and meanwhile, under the suction action of fans (comprising an external discharge flue gas fan 21-1, a high NOx flue gas fan 21-2, a desulfurization flue gas fan 21-3 and a low temperature flue gas fan 21-4), sintering airflow enters from the upper part of the sinter bed 2 and penetrates through the sinter mixture 2.1 and a bed charge 2.2, and a grate of the sintering trolley 1.1 enters an air box 12.
Adjusting the operation technological parameters of the sintering machine 1, reducing the thickness of the sinter bed 2 by 10 percent from original 800mm to 720mm, or reducing the traveling speed of a sintering machine trolley 1.1 by 10 percent, and correspondingly reducing the air suction volume of fans (comprising an external exhaust flue gas fan 21-1, a high NOx flue gas fan 21-2, a desulfurization flue gas fan 21-3 and a low temperature flue gas fan 21-4). The relative lengths of 5 areas such as an ignition area, a low-temperature smoke area, a smoke rapid heating area, a NOx concentration rapid reduction area and a high-temperature smoke area of the original sintering machine are adjusted and changed, the length of the high-temperature smoke area is increased to 40-45% of the total length of the sintering machine 1 after adjustment, and the length of the low-temperature smoke area is shortened to 38-43% of the total length of the sintering machine 1, so that sintering smoke collected by a low-temperature smoke main flue 16-3 can completely enter the high-temperature smoke area.
Collecting sintering flue gas in a flue gas rapid temperature rise area and a NOx concentration rapid reduction area through a high NOx flue gas main flue 16-2, removing dust through a high NOx flue gas dust remover 18-2 after collection, supplementing oxygen, entering an oxygen mixer 11-2 for mixing, entering a high NOx flue gas circulating cover 3-2 above a sintering material layer 2 in a low temperature flue gas area through a high NOx flue gas pipeline 6-2 under the action of a high NOx flue gas fan 21-2, entering the sintering material layer 2 again for sintering under the suction action of a desulfurization flue gas fan 21-3 corresponding to the low temperature flue gas area, and simultaneously performing SO (sulfur oxide) sintering 2 And enriching pollutants such as NOx.
The high NOx flue gas circulation cover 3-2 covers the low-temperature flue gas area and 1-2 groups of air boxes 12 in the flue gas rapid heating area close to the low-temperature flue gas area, and the flue gas outlets of the 1-2 groups of air boxes 12 and the flue gas outlets of 2-4 groups of air boxes 12 in the low-temperature flue gas area close to the flue gas rapid heating area are respectively connected with a low-temperature flue gas main flue 16-3 and a high NOx flue gas main flue 16-2 through an exchange valve 17; the circulation pattern of the flue gas (i.e. the ratio of the internal circulation amount to the external circulation amount) and the flue gas circulation amount are adjusted by the exchange valves 17 at the outlets of the 3-6 groups of windboxes. The exchange valves 17 at the outlets of the 3-6 groups of air boxes are all adjusted to be communicated with the flue gas channel and the high NOx flue gas main flue 16-2, so that the internal circulation volume is increased, the enrichment multiple of pollutants in the flue gas is improved, and the external discharge volume of the flue gas is reduced. At the moment, SO in the sintering flue gas led out from the low-temperature flue gas main flue 16-3 2 Can reach 3000mg/m 3 The concentration of NOx can reach 1000mg/m 3 The specific numerical values fluctuate slightly depending on the raw materials.
The sintering flue gas led out from the low-temperature flue gas main flue 16-3 is in a saturated humidity state, and the temperature is lower and is 70-80 ℃. The flue gas is dedusted by a desulfurization flue gas deduster 22 and then enters an ammonia desulfurization system 15 for desulfurization. The desulfurized flue gas keeps high ammonia escape amount, and the molar ratio of the ammonia content to NOx in the flue gas is kept between 0.8 and 0.9.
The desulfurized flue gas containing high ammonia escape amount is sent into the low-temperature flue gas circulating cover 3-1 through the low-temperature flue gas pipeline 6-1 under the action of the desulfurized flue gas fan 21-3. The low-temperature flue gas circulating cover covers the high-temperature flue gas area and the 1-2 groups of air boxes 12 in the NOx concentration rapid reduction area adjacent to the high-temperature flue gas area, and flue gas outlets of the 1-2 groups of air boxes 12 and flue gas outlets of the 2-4 groups of air boxes 12 in the high-temperature flue gas area adjacent to the flue gas NOx concentration rapid reduction area are respectively connected with a high-temperature flue gas main flue 16-3 and a high-NOx flue gas main flue 16-2 through an exchange valve 17; the circulation pattern of the flue gas (i.e. the ratio of the internal circulation amount to the external circulation amount) and the flue gas circulation amount are adjusted by the exchange valves 17 at the outlets of the 3-6 groups of windboxes. And all the exchange valves 17 at the outlets of the 3-6 groups of air boxes are adjusted to be communicated with the flue gas channel and the high-NOx flue gas main flue 16-2, so that the internal circulation amount is increased, and the flue gas amount entering the high-temperature flue gas main flue 16-1 is reduced. At the moment, the amount of the discharged flue gas is about 35 percent of the total amount of the original sintering flue gas.
The high-temperature flue gas collected by the high-temperature flue gas main flue 16-1 is dedusted by the high-temperature flue gas deduster 18-1, enters the waste heat boiler 19 to recover waste heat, is further dedusted by the exhaust flue gas deduster 20, and is exhausted.
Example 2
See FIG. 2, 450m from a certain Steel works 2 The strand sintering machine of (1) has 24 groups (48) of windboxes 12 in total. Adjusting the operation process parameters of the sintering machine 1, reducing the thickness of the sinter bed 2 by 10 percent from original 800mm to 720mm, or reducing the traveling speed of a sintering machine trolley 1.1 by 10 percent, and correspondingly reducing the air suction volume of fans (comprising an external exhaust flue gas fan 21-1, a high NOx flue gas fan 21-2, a desulfurization flue gas fan 21-3 and a low temperature flue gas fan 21-4). The relative lengths of 5 areas such as an ignition area, a low-temperature smoke area, a smoke rapid heating area, a NOx concentration rapid reduction area and a high-temperature smoke area of the original sintering machine are adjusted and changed, the length of the high-temperature smoke area is increased to 40-45% of the total length of the sintering machine 1 after adjustment, and the length of the low-temperature smoke area is shortened to 38-43% of the total length of the sintering machine 1, so that sintering smoke collected by a low-temperature smoke main flue 16-3 can completely enter the high-temperature smoke area.
The sintering flue gas in the low-temperature flue gas area is collected through a low-temperature flue gas main flue 16-3, the sintering flue gas in the rapid flue gas temperature rising area and the rapid NOx concentration reducing area is collected through a high-NOx flue gas main flue 16-2, and the sintering flue gas in the high-temperature flue gas area is collected through a high-temperature flue gas main flue 16-1.
Sintering flue gas collected by the low-temperature flue gas main flue 16-3 enters the low-temperature flue gas pipeline 6-1 after being dedusted by the low-temperature flue gas deduster 18-3, and ammonia water is sprayed into the low-temperature flue gas pipeline 6-1 through 1-3 layers of ammonia water nozzles 14.1 arranged along the circumferential direction to form ammonia water mist 14.2. The ammonia gas formed by gasification and the sintering flue gas enter an ammonia gas mixer 11-1 to be mixed, and then are sent into a low-temperature flue gas circulating cover 3-1 through a low-temperature flue gas pipeline 6-1 under the action of a low-temperature flue gas fan 20-4. The molar ratio of the ammonia amount injected by the ammonia water nozzle 14.1 to the NOx content in the flue gas is kept between 3.0 and 4.0.
The sintering flue gas entering the high-temperature flue gas main flue 16-1 is dedusted by the high-temperature flue gas deduster 18-1, then enters the waste heat boiler 19 for waste heat recovery, then enters the desulfurization flue gas deduster 22 for further dedusting, and then enters the desulfurization system 15.
The rest is the same as embodiment 1.
The technical scheme reduces the external discharge capacity of sintering flue gas by over 55 percent.
Claims (15)
1. An online denitration process for sintering flue gas comprises the steps that sintering airflow enters a sintering material layer to support combustion and sinter under the suction action of a fan to form sintering flue gas, and the sintering flue gas passes through the sintering material layer, a sintering machine trolley grate and an air box below a trolley and enters a main flue; the sintering machine is sequentially divided into an ignition area, a low-temperature flue gas area, a flue gas rapid heating area, a NOx concentration rapid reduction area and a high-temperature flue gas area by 5 areas along the travelling direction of a sintering machine trolley; the method is characterized in that sintering flue gas is collected through 3 main flues including a low-temperature flue gas main flue, a high-NOx flue gas main flue and a high-temperature flue gas main flue respectively, wherein the ignition area accounts for 2-3 bellows, the low-temperature flue gas area accounts for 50-55% of the total length of the sintering machine, the flue gas rapid heating area accounts for 10-15% of the total length of the sintering machine, the NOx concentration rapid reduction area accounts for 10-15% of the total length of the sintering machine, and the high-temperature flue gas area accounts for 15-20% of the total length of the sintering machine; the low-temperature flue gas main flue correspondingly collects sintering flue gas in an ignition region and a low-temperature flue gas region, the high-NOx flue gas main flue correspondingly collects sintering flue gas in a flue gas rapid heating region and a NOx concentration rapid reducing region, and the high-temperature flue gas main flue correspondingly collects sintering flue gas in a high-temperature flue gas region; 2-4 groups of air box smoke outlets of the low-temperature smoke area, which are close to the smoke rapid heating area, are respectively connected with a low-temperature smoke main flue and a high NOx smoke main flue through exchange valves; 2-4 groups of air box smoke outlets adjacent to the high-temperature smoke area and the NOx concentration rapid reduction area are respectively connected with a high-NOx smoke main flue and a high-temperature smoke main flue through exchange valves; and the sintering flue gas collected by the low-temperature flue gas main flue is mixed with ammonia gas, the mixture is introduced into a low-temperature flue gas circulation cover above a sintering material layer in a high-temperature flue gas area through a low-temperature flue gas pipeline, enters the sintering material layer again under the suction action of a fan, is heated in the sintering material layer, and NOx in the sintering flue gas and the ammonia are subjected to reduction denitration reaction under the catalytic action of iron-based polyoxide rich in the sintering material layer.
2. The on-line denitration process of the sintering flue gas as claimed in claim 1, wherein at least 1 layer of ammonia water or liquid ammonia nozzles are circumferentially arranged on the side wall of the low-temperature flue gas pipeline, the nozzles eject ammonia water or liquid ammonia, and the molar ratio of the amount of ammonia contained in the ejected ammonia water or liquid ammonia to the NOx content in the sintering flue gas is 0.8-0.9; the ammonia water or the liquid ammonia is gasified into ammonia gas in the sintering flue gas and enters the ammonia gas mixer together with the sintering flue gas to be mixed, and the sintering flue gas and the ammonia gas are mixed and then enter the low-temperature flue gas circulation cover above the sintering material layer in the high-temperature flue gas area.
3. The online denitration process of the sintering flue gas as claimed in claim 1, wherein the sintering flue gas of the low-temperature flue gas main flue is introduced into a low-temperature flue gas circulation cover above a sinter bed in a high-temperature flue gas region through a low-temperature flue gas pipeline after being introduced into an ammonia desulphurization system for desulphurization.
4. The online denitration process of sintering flue gas as claimed in claim 3, wherein the depth of ammonia water of the desulphurization absorbent of the ammonia desulphurization system is increased to increase the ammonia escape amount, and the molar ratio of the ammonia escape amount to the NOx content in the sintering flue gas is controlled to be 0.8-0.9.
5. The online denitration process of the sintering flue gas as claimed in claim 1, wherein the sintering flue gas from the high-NOx flue gas main flue is sent into a high-NOx flue gas circulation cover above a sintering material layer in a low-temperature flue gas area through a high-NOx flue gas pipeline, and enters the sintering material layer again for circulation under the suction effect of a fan.
6. The on-line denitration process for the sintering flue gas as claimed in claim 5, wherein oxygen is supplemented to the flue gas in the main flue of the high NOx flue gas, and the flue gas is mixed by an oxygen mixer and then enters the high NOx flue gas circulation cover.
7. The online denitration process of sintering flue gas as claimed in claim 5, wherein a plurality of air flow balance pipes are uniformly distributed on the low temperature flue gas circulation cover and the high NOx flue gas circulation cover, a one-way flap valve is mounted on the air flow balance pipes, and air passes through the flap valve from top to bottom through the balance pipes to enter a sinter bed.
8. The online denitration process for the sintering flue gas as claimed in claim 1, wherein the sintering flue gas from the high-temperature flue gas main flue enters a flue gas desulfurization system after dust removal and waste heat recovery.
9. The online denitration process for sintering flue gas as claimed in claim 5, wherein the high NOx flue gas circulation cover covers the low temperature flue gas region and a part of the flue gas rapid temperature rise region which is close to the low temperature flue gas region.
10. The online denitration process for sintering flue gas as claimed in claim 1, wherein the low-temperature flue gas circulation cover covers the high-temperature flue gas area and a part of NOx concentration rapid reduction area which is close to the high-temperature flue gas area.
11. The online denitration process of sintering flue gas as claimed in claim 1, wherein the trolley and the sintering mixture run from the head to the tail in an inclined manner, the sintering gas flow and the sintering flame front are perpendicular to the travelling direction of the trolley and obliquely pass through the sintering material layer downwards.
12. The online denitration process for sintering flue gas as claimed in claim 1 or 11, wherein the trolley and the sintering mixture on the trolley run from the head to the tail in an inclined manner, and the inclination is 5-15%.
13. The on-line denitration process for sintering flue gas as claimed in claim 5, wherein a plurality of temperature monitors are installed at the inner side of the edges of the high NOx flue gas circulation cover and the low temperature flue gas circulation cover, and monitoring signals are interlocked with the high NOx flue gas circulation fan and the low temperature flue gas exhaust fan.
14. The on-line denitration process of sintering flue gas as claimed in claim 13, wherein when the temperature monitor monitors that the temperature of the gas flow is higher than the room temperature, the bellows flue gas outlet exchange valve connecting the two main flues is switched to adjust the amount of sintering flue gas entering the flue gas main flue.
15. The on-line denitration process of sintering flue gas as claimed in claim 13, wherein when the temperature monitor monitors that the temperature of the gas flow is higher than the room temperature, the air suction volume of the fan connected to the corresponding flue gas main flue is adjusted.
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Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5482304A (en) * | 1977-12-14 | 1979-06-30 | Sumitomo Metal Ind Ltd | Nox decreasing method in manufacture of sintered ore |
| DE3442967A1 (en) * | 1984-11-24 | 1986-05-28 | GEA Luftkühlergesellschaft Happel GmbH & Co, 4630 Bochum | Apparatus for the denitration of flue gas |
| JP2001241863A (en) * | 2000-02-29 | 2001-09-07 | Kobe Steel Ltd | Exhaust gas circulating sintering operation method |
| CN101024143A (en) * | 2007-01-12 | 2007-08-29 | 中冶长天国际工程有限责任公司 | Sinter-smoke circulation collected desulfurizing method and apparatus |
| CN102242257A (en) * | 2011-06-30 | 2011-11-16 | 中南大学 | Flue gas circulation and biomass energy combined iron ore sintering method |
| CN104132550A (en) * | 2014-07-01 | 2014-11-05 | 中国科学院过程工程研究所 | Energy-saving environment-friendly sintering waste gas waste-heat utilization and pollutant purification process and system |
| CN203935781U (en) * | 2014-07-18 | 2014-11-12 | 温广胜 | The high oxynitrides flue gas recirculation of sintering machine denitrating system |
| CN104195326A (en) * | 2014-08-19 | 2014-12-10 | 浙江大学 | Sintering energy-saving technique and system capable of removing multiple pollutants |
| CN105135895A (en) * | 2015-08-03 | 2015-12-09 | 郑琨 | Selective sintering flue gas sectional type comprehensive treatment technology |
| CN105889884A (en) * | 2016-04-19 | 2016-08-24 | 南京师范大学 | System for increasing temperature of sintering flue gas, conducting selective catalytic reduction (SCR) denitration through sintering flue gas and generating steam through waste heat |
| CN107029554A (en) * | 2017-06-13 | 2017-08-11 | 武汉钢铁有限公司 | Flue gas recirculation denitrating system based on sintering flue gas self-catalysis |
| CN107166971A (en) * | 2017-06-13 | 2017-09-15 | 武汉钢铁有限公司 | Sinter the low NO of flue gas recirculationxDischarge technology |
-
2019
- 2019-09-27 CN CN201910924302.0A patent/CN112569758B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5482304A (en) * | 1977-12-14 | 1979-06-30 | Sumitomo Metal Ind Ltd | Nox decreasing method in manufacture of sintered ore |
| DE3442967A1 (en) * | 1984-11-24 | 1986-05-28 | GEA Luftkühlergesellschaft Happel GmbH & Co, 4630 Bochum | Apparatus for the denitration of flue gas |
| JP2001241863A (en) * | 2000-02-29 | 2001-09-07 | Kobe Steel Ltd | Exhaust gas circulating sintering operation method |
| CN101024143A (en) * | 2007-01-12 | 2007-08-29 | 中冶长天国际工程有限责任公司 | Sinter-smoke circulation collected desulfurizing method and apparatus |
| CN102242257A (en) * | 2011-06-30 | 2011-11-16 | 中南大学 | Flue gas circulation and biomass energy combined iron ore sintering method |
| CN104132550A (en) * | 2014-07-01 | 2014-11-05 | 中国科学院过程工程研究所 | Energy-saving environment-friendly sintering waste gas waste-heat utilization and pollutant purification process and system |
| CN203935781U (en) * | 2014-07-18 | 2014-11-12 | 温广胜 | The high oxynitrides flue gas recirculation of sintering machine denitrating system |
| CN104195326A (en) * | 2014-08-19 | 2014-12-10 | 浙江大学 | Sintering energy-saving technique and system capable of removing multiple pollutants |
| CN105135895A (en) * | 2015-08-03 | 2015-12-09 | 郑琨 | Selective sintering flue gas sectional type comprehensive treatment technology |
| CN105889884A (en) * | 2016-04-19 | 2016-08-24 | 南京师范大学 | System for increasing temperature of sintering flue gas, conducting selective catalytic reduction (SCR) denitration through sintering flue gas and generating steam through waste heat |
| CN107029554A (en) * | 2017-06-13 | 2017-08-11 | 武汉钢铁有限公司 | Flue gas recirculation denitrating system based on sintering flue gas self-catalysis |
| CN107166971A (en) * | 2017-06-13 | 2017-09-15 | 武汉钢铁有限公司 | Sinter the low NO of flue gas recirculationxDischarge technology |
Non-Patent Citations (3)
| Title |
|---|
| 中国钢铁行业重点工序烟气超低排放技术进展;于勇;《钢铁》;20190915;1-11 * |
| 烧结烟气分段式综合处理新工艺的设计;郑琨;《钢铁研究》;20160410(第02期);41-44 * |
| 钢铁工业NOx控制技术创新和应用;刘文权;《技术与工程应用》;20141130;25-34 * |
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