CN213725710U - Sintering flue gas coprocessing system - Google Patents
Sintering flue gas coprocessing system Download PDFInfo
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- CN213725710U CN213725710U CN202022557533.3U CN202022557533U CN213725710U CN 213725710 U CN213725710 U CN 213725710U CN 202022557533 U CN202022557533 U CN 202022557533U CN 213725710 U CN213725710 U CN 213725710U
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Abstract
The utility model relates to a sintering flue gas cooperative processing system, cooperative processing system includes flue gas pipeline and the interior hot type reactor, cyclone, rapid cooling ware, desulfurizing tower, dust remover, draught fan and the outer row's of gas device who establishes ties in proper order according to flue gas direction of delivery. The utility model can realize the cooperative disposal of various pollutants, the internal heating type reactor effectively controls the discharge amount of carbon monoxide, and simultaneously reduces the pollution of dioxin; the heat released by the combustion of the carbon monoxide and the dioxin further assists the treatment of other pollution components by the internal thermal reactor; the utility model provides a denitration mode of system disposal adopts direct reduction denitration and nitrogen reduction denitration simultaneously, and the denitration stability is good, the cost is low and the efficiency is high; the utility model provides a coprocessing system's accessory substance is stable composition such as calcium sulfate, does not produce unstable composition such as calcium sulfite, and the accessory substance can be used as the cement raw materials, has realized the dual environmental protection benefit of solid useless processing.
Description
Technical Field
The utility model relates to a clean technical field particularly, relates to a sintering flue gas concurrent processing system.
Background
With the continuous development of the heavy industry in China, the problem of environmental pollution is more and more serious, and in the heavy industry, the steel industry is the basic industry in China and is also one of the main industries increasing the environmental pollution. Its sintering flue gas SO2The discharge amount already accounts for the whole industrial SO2The emission is about 12 percent, which is SO in the steel industry2The air pollution treatment standard of an important pollution control object is continuously improved, the ultralow emission of the steel industry is gradually promoted, and the requirement of SO2The discharge concentration is not higher than 35mg/Nm3。
At present, sintering flue gas desulfurization technology can be divided into wet desulfurization, semi-dry desulfurization and dry desulfurization according to the physical state of an absorbent. The limestone-gypsum desulfurization system in wet desulfurization is the most mature flue gas desulfurization process at present, and the process takes limestone or lime slurry as a desulfurizing agent to remove SO in an absorption tower2Spraying and washing the flue gas to ensure that SO in the flue gas2Reaction to produce CaSO3And CaSO4Simultaneously blowing air into the slurry in the absorption tower to force the CaSO3Are all oxidized into CaSO4The by-product of the desulfurization is gypsum. And meanwhile, air is blown to generate more uniform slurry, so that the desulfurization rate is easy to reach 90%, and scaling and blockage are easy to control. The main advantages of the limestone/gypsum process are: the applicable coal variety range is wide, the desulfurization efficiency is high (when some devices Ca/S are equal to 1, the desulfurization efficiency is more than 90%), the utilization rate of the absorbent is high (can be more than 90%), the operation rate of the device is high (can reach more than 90%), the working reliability is high, and the source of the desulfurizer-limestone is rich and cheap. However, the disadvantages of the limestone/gypsum process are also evident: high initial investment cost, high running cost, large floor area, complex system management and operation, and high abrasion resistanceThe corrosion phenomenon is serious, the byproduct gypsum is difficult to treat, and the waste water is difficult to treat.
The dry desulfurization is to remove SO in flue gas by using powdery or granular absorbent, adsorbent or catalyst2The gas, different dry desulfurizing agents, operate in different temperature zones, and thus can be divided into low-temperature (normal temperature and less than 100 ℃) desulfurizing agents, medium-temperature (100 ℃ -400 ℃) desulfurizing agents and high-temperature (C>400 ℃ desulfurizing agent, which has the defects that the utilization rate of the absorbent is lower than that of a wet desulphurization process, the removal effect of the absorbent for high-sulfur sintering flue gas is poorer, the comprehensive utilization of final products is influenced by the mixing of fly ash and desulphurization products, and the reaction in an absorption tower is incomplete to generate unstable products.
The mature semi-dry desulfurization process comprises an NID dry desulfurization technology, and the technical parameters are as follows: calcium-sulfur ratio (Ca/S):<1.4; material cycle times: 30-150 parts of; desulfurization efficiency: 70% -80%; desulfurized SO2Removing efficiency:>99 percent; dust removal efficiency:>99.9 percent; the availability of the system:>1 percent. The CFB circulating fluidized bed flue gas desulfurization technology comprises the following technical parameters: technical parameters calcium-sulfur ratio (Ca/S):<1.4; material cycle times: 30-100 parts; desulfurization efficiency:>80％；SO2removing efficiency:>99 percent; dust removal efficiency:>99.9 percent; the availability of the system:>98％。
the semi-dry desulphurization can generate a large amount of calcium sulfite, and the calcium sulfite is an unstable substance and easily causes secondary pollution to the environment. The product components of the existing semi-dry desulfurization process are difficult to reuse, and are generally treated in a stacking or landfill mode, so that the treatment can reduce the disposal cost of waste, but is not an environment-friendly treatment means. And the prior semi-dry desulfurization process has low utilization rate of the absorbent, and the absorbent mixed in the final product can not be effectively recycled, thereby causing a great deal of waste and secondary pollution of the absorbent.
Except SO in sintering flue gas2Usually, 5000-15000mg/Nm3At present, the treatment of CO in the sintering flue gas is a blank, so that the surplus energy of CO cannot be recovered, energy waste is caused, and meanwhile, the emission of CO also causes atmospheric pollution.
Theoretically, feasible CO removing methods comprise a catalytic oxidation method and a flameless combustion oxidation method, and compared with the catalytic oxidation method, the flameless combustion oxidation method can adapt to more complex sintering smoke components, avoids catalyst poisoning caused by harmful components, and can synchronously remove dioxin while carrying out flameless combustion on CO, so that the flameless combustion oxidation method has better industrial prospect.
The existing CO flameless combustion processing technology is relatively mature in application of a waste gas incinerator, and the principle is that the temperature of CO-containing sintering flue gas is raised to a reaction temperature by using heat generated by combustion of auxiliary fuel, so that oxidative decomposition is generated. For the combustion process of CO in the waste gas incinerator, the requirement of the lowest ignition temperature is met, and the ignition area is limited, so that the CO cannot be violently combusted below the lowest ignition temperature; but in the ignition area, the ignition speed increases along with the temperature rise, the temperature continues to rise, and the conversion rate curve is transited from gentle to steep, namely, an inflection point exists. The CO combustion process goes from non-combustible (<639 ℃) to a start-up to a violent combustion. The ignition temperature of the sintering flue gas CO is 639 ℃, the deflagration temperature is 700-710 ℃, and the ignition stage is 639-700 ℃. According to related data, the combustion of CO at the deflagration temperature (710 ℃) is only 0.05s, and the engineering design can be designed according to 1-2 s.
Except for SO2Besides CO, the sintering flue gas also comprises nitrogen oxides, wherein the ultralow emission of the steel industry is gradually promoted, and the emission concentration of NOx is required to be not higher than 50mg/Nm3The prior denitration process comprises an SCR denitration process and an SNCR denitration process, wherein the SCR denitration process refers to that ammonia gas selectively reacts with nitrogen oxide through reduction and desorption reaction under the action of a catalyst and in the presence of oxygen to generate nitrogen and water, but does not react with oxygen in flue gas through oxidation. However, the SCR denitration process is prone to poisoning of the cyanamide sulfite catalyst and clogging of the heat exchanger, and cannot remove carbon monoxide and dioxin from flue gas. The SNCR denitration process is characterized in that ammonia or urea and other amino groups are uniformly sprayed into a flue in the front of a separator under the condition of not adopting a catalystThe reducing agent is rapidly decomposed in the furnace and reacts with nitrogen oxides in the flue gas to generate nitrogen and water, so that the aim of denitration is fulfilled.
In the prior art, for the removal of different pollutants, in order to ensure the removal effect, a mode of independent removal and sequential treatment is usually adopted, and a cooperative treatment system and a method capable of realizing 'one-time treatment and synchronous removal' of different pollutants are lacked.
In view of this, the utility model is especially provided.
Disclosure of Invention
The utility model discloses make the improvement to sintering flue gas environmental protection processing system, this system can also realize getting rid of carbon monoxide and dioxin when realizing desulfurization, denitration to the beneficial effect of solid useless of coprocessing.
The utility model aims at providing a sintering flue gas cooperative processing system, desorption when this sintering flue gas cooperative processing system can realize sulfur oxide, nitrogen oxide, carbon monoxide and the dioxin that contains in the flue gas, avoids the secondary pollution that solid useless caused simultaneously to the multiple component gets rid of the synergism effect that the in-process realized promoting mutually.
Another object of the utility model is to provide a sintering flue gas concurrent processing method, this method uses above-mentioned sintering flue gas concurrent processing system, can reduce multiple harmful component content in the sintering flue gas to below the standard value simultaneously, avoids the secondary pollution that solid useless caused simultaneously.
The utility model discloses still another purpose provides the application of above-mentioned sintering flue gas concurrent processing system in sintering flue gas is handled and pelletizing flue gas is handled.
In order to achieve the purpose, the utility model provides a sintering flue gas cooperative processing system, which comprises a flue gas conveying pipeline and equipment connected in series by the flue gas conveying pipeline, wherein the equipment sequentially comprises an internal heating type reactor, a cyclone dust collector, a rapid cooler, a desulfurizing tower, a dust collector, an induced draft fan and a gas external exhaust device according to the flue gas conveying direction; the bottom of the desulfurization tower is also provided with a separator; at least one solid waste conveying pipeline is arranged between the devices, and the solid waste conveying direction in the solid waste conveying pipeline is opposite to the flue gas conveying direction; the bottom of the internal heating type reactor is provided with a booster fan and a combustion-supporting air pipeline, and the combustion-supporting air pipeline is connected with the combustion-supporting fan; an SNCR denitration device is arranged between the internal heating type reactor and the cyclone dust collector; an SCR denitration device is arranged in the rapid cooler; the internal heating type reactor is also connected with a fuel supply device.
Preferably, the gas discharge device comprises an atmospheric discharge device; further preferably, the gas discharge device comprises a chimney.
The solid waste conveying pipeline can convey solid waste containing a large amount of calcium sulfite generated after the sintering flue gas is desulfurized back to the upstream treatment system, so that secondary treatment of the solid waste is realized, meanwhile, the reduction capacity of the calcium sulfite is utilized, primary treatment is carried out on the sintering flue gas, the solid waste is fully utilized, and a remarkable synergistic effect is formed between solid waste treatment and sintering flue gas treatment.
The internal heating reactor adopts combustible gas such as carbon-containing solid waste or blast furnace gas and the like as a heat source to heat the sintering flue gas, so that CO and dioxin in the sintering flue gas are removed after oxidation combustion, and simultaneously, heat is additionally released, and the removal treatment of sulfur components in the sintering flue gas by the once-treated solid waste is further promoted. The booster fan and the combustion-supporting air duct pipe at the bottom of the internal thermal reactor can simultaneously blow sintering flue gas, and the control of the retention time of the sintering flue gas in the internal thermal reactor is realized by adjusting the flow and the flow velocity of the sintering flue gas, so that the subsequent adjustment of the removal effect of various components is realized. The temperature in the internal thermal reactor is rapidly raised to the combustion temperature of CO by the heat released by the combustion of the combustible components, and the combustion of the CO further raises the temperature in the internal thermal reactor, so that the conversion process of SNCR treatment and primary solid waste to secondary solid waste is promoted, thereby realizing the sufficient absorption of various gases and obtaining the effect of synergistic treatment.
In an optional embodiment, the fuel is solid waste fuel, a solid waste fuel storage device is arranged at the upstream of the internal thermal reactor, a solid waste conveying pipeline is arranged between the solid waste fuel storage device and the bottom of the dust remover, and a heat source is provided for heating the sintering flue gas by adding and igniting carbon-containing solid waste fuel into the internal thermal reactor.
Preferably, the solid waste fuel storage device (3) is connected with the internal heating type reactor (5) through a feeding device (16).
In an alternative embodiment, the fuel is a combustible gas, and the internal thermal reactor is provided with at least one gas combustion device, and the combustible gas is ignited to provide heat for heating the sintering flue gas.
Preferably, the combustible gas comprises blast furnace gas;
further preferably, the blast furnace gas comprises steel plant blast furnace gas.
In an optional embodiment, the SCR denitration device is arranged in a region with the temperature of 350-400 ℃ in the rapid cooler.
On the other hand, the utility model also provides a method of adopting above-mentioned sintering flue gas coprocessing system to carry out coprocessing, coprocessing method includes, divide into two parts with pending sintering flue gas, enters interior hot type reactor through booster fan and combustion-supporting fan drum respectively, and the burning back flows along flue gas pipeline, finally discharges after gaseous outer discharge device realizes handling, and the primary solid waste who produces carries out secondary treatment in the upstream facilities of flue gas direction of delivery is carried back to through solid useless pipeline transport to the coprocessing process in the coprocessing process.
Preferably, the sintering flue gas comprises sintering machine head flue gas.
In a possible embodiment, the sintering flue gas is subjected to an internal thermal reactor in a pulsed manner under the action of a combustion fan.
In a feasible implementation mode, the temperature in the internal thermal reactor (5) is adjusted to be 800-1050 ℃, and the oxygen content in the space below the combustion-supporting air pipeline (4) in the internal thermal reactor (5) is less than 2%.
In the space below a combustion air pipeline of the internal thermal reactor, oxidation and reduction reactions simultaneously exist in nitrogen oxides carried in sintering flue gas, when the temperature is controlled below 1050 ℃, and the oxygen content of the sintering flue gas is less than 2%, the reduction rate of the nitrogen oxides is greater than the oxidation rate, so that the nitrogen oxides with the volume fraction of 70% can be reduced into nitrogen and water in the internal thermal reactor, and the oxygen content includes but is not limited to 0.5%, 1%, 1.5% or 1.8%.
In feasible embodiment, gas velocity of flow 20 ~ 30m/s in the connecting channel between interior hot type reactor and the cyclone, the utility model discloses have narrow intercommunication pipeline between well interior hot type reactor and the cyclone, sintering flue gas in the interior hot type reactor forms high-pressure gas under booster fan and the exothermic combined action of burning, and the cyclone space is huge, the atmospheric pressure is low, consequently, the gas velocity of flow in the intercommunication pipeline between interior hot type reactor and the cyclone increases suddenly. Set up SNCR denitrification facility here, then can make sintering flue gas and denitrifier intensive mixing through adjustment gas velocity of flow to improve denitration reaction efficiency, guarantee the ammonia in the flue 800 ~ 1050 ℃ temperature interval in dwell time not less than 5 seconds simultaneously.
In a possible embodiment, the cooling rate of the rapid cooler is 200 ℃/s to 300 ℃/s.
Above-mentioned rapid cooling ware can be in 4s time, will spin the sintering flue gas in the wind dust remover and follow 900 ℃ of cooling to 140 ℃, through the regulation of water supply capacity, can the not co-altitude temperature value in the accurate control rapid cooling ware, therefore, can be according to the high sensitivity of SCR denitrification facility to the temperature, set up the temperature window in the inside 350 ~ 400 ℃ of rapid cooling ware position, and add and establish SCR denitrification facility, utilize the ammonia that escapes among the SNCR denitrification facility and the nitrogen oxide reaction realization denitration in the sintering flue gas, make the nitre content in the sintering flue gas reach national emission standard.
The third aspect of the invention provides an application of the sintering flue gas co-processing system and/or the sintering flue gas co-processing method in sintering flue gas processing and/or pelletizing flue gas processing.
The utility model discloses gain beneficial effect as follows:
the utility model can realize the cooperative disposal of various pollutants, the internal heating type reactor effectively controls the discharge amount of carbon monoxide, and simultaneously reduces the pollution of dioxin; and the heat of carbon monoxide and dioxin burning release has further assisted the processing of interior hot type reactor to other solid wastes again, the utility model provides a stable composition such as calcium sulfate is to the accessory substance of coprocessing system, does not produce unstable composition such as calcium sulfite, and the accessory substance can be used as the cement raw materials, and the solid useless ability of coprocessing of interior hot type reactor has dual environmental protection benefit.
Dioxin exists in sintering flue gas, and the solid waste fuel can also generate the dioxin during combustion, and the conventional content of the dioxin in the flue gas entering the internal heating type reactor is 3-50ng-TEQ/Nm3. Dioxin is a chloro-oxygenated tricyclic aromatic compound, can be completely decomposed at a temperature range of 850-1000 ℃, and can be fully synthesized again after staying for 4-5 seconds at a temperature range of 200-400 ℃. The utility model discloses in the flue gas temperature was in 850 ~ 1000 ℃'s scope in making furnace for solid useless fuel burning release heat to the dioxin treatment mode in the sintering flue gas, the dioxin in the flue gas decomposes completely like this to in converging rapid cooling ware along with the flue gas. The rapid cooler is used for reducing the temperature of the flue gas, the temperature of the flue gas is reduced to 450 ℃ after the flue gas reaches a distance before the outlet of the rapid cooler, at the moment, the rapid cooling design is adopted in the temperature section, so that the time for reducing the temperature of the flue gas from 450 ℃ to below 200 ℃ is shortened to below 2s, the retention time of dioxin in a resynthesis temperature interval is greatly shortened, the great regeneration of the dioxin is inhibited, and finally the content of the dioxin is controlled to be 0.3ng-TEQ/Nm3The purpose of removing dioxin is achieved as follows.
Carbon monoxide exists in the sintering flue gas, and solid waste fuel can be generated when the solid waste fuel is incompletely combusted below a combustion-supporting air pipeline, and the content of the carbon monoxide in the flue gas is less than 1 percent and far lower than the explosion limit (more than 10 percent). The carbon monoxide has an ignition point of over 800 ℃ under the condition of sufficient oxygen. The utility model discloses oxygen content is sufficient in the interior hot type reactor of well, and carbon monoxide in the flue gas burns completely in 850 ~ 1000 ℃ of temperature interval and generates carbon dioxide, and can not produce once more.
The utility model discloses the following partial temperature control of combustion-supporting wind pipeline of interior hot type reactor is below 1050 ℃, and the flue gas oxygen content of this part is < 2%, and when the oxygen content was less than 2%, atmosphere in this region is oxidation and reduction coexisted, and the nitrogen oxide that brings in this region sintering flue gas is reduced to nitrogen and water, has improved the stability of denitration efficiency and denitration, has reduced the consumption of denitrifier to the consumption of denitration catalyst has been reduced, and the denitration cost is lower, more environmental protection.
Other features and advantages of the present invention will be described in detail in the detailed description which follows.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention, and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
Fig. 1 is a system for co-processing sintering flue gas provided by embodiment 1 of the present invention.
Icon: 1 is combustion fan, 2 is booster fan, 3 is solid useless fuel storage device, 4 is combustion-supporting wind pipeline, 5 is interior hot type reactor, 6 is cyclone, 7 is rapid cooling device, 8 is the desulfurizing tower, 9 is the dust remover, 10 is the chimney, 11 is the draught fan, 12 is solid useless pipeline, 13 is the separator, 14 is SNCR denitrification facility, 15 is SCR denitrification facility, 16 is feeder, 17 is gas combustion device, A is the ash bin.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the drawings in the embodiments of the present invention are combined below to clearly and completely describe the technical solutions in the embodiments of the present invention. It is to be understood that the embodiments described are only some of the embodiments of the present invention, and not all of them. The components of embodiments of the present invention, as generally described and illustrated in the figures herein, may be arranged and designed in a wide variety of different configurations.
In the description of the present invention, it should be noted that the terms "inside" and "outside" are used for indicating the position or positional relationship based on the position or positional relationship shown in the drawings or the position or positional relationship that the product of this application is usually placed when in use, and are only for convenience of describing the present invention and simplifying the description, but not for indicating or implying that the device or element to be referred must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like are used merely to distinguish one description from another, and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
The embodiment provides a sintering flue gas co-processing system, as shown in fig. 1, which includes a flue gas conveying pipeline and equipment connected in series by the flue gas conveying pipeline, wherein the equipment sequentially includes an internal heating type reactor 5, a cyclone dust collector 6, a rapid cooler 7, a desulfurizing tower 8, a dust collector 9, an induced draft fan 11 and a chimney 10 according to a flue gas conveying direction; the bottom of the desulfurizing tower 8 is also provided with a separator 13; the bottom of the internal heating type reactor 5 is provided with a booster fan 2 and a combustion-supporting air pipeline 4, and the combustion-supporting air pipeline 4 is connected with a combustion-supporting fan 1; a solid waste fuel storage device 3 is further arranged at the upstream of the internal thermal reactor 5, the solid waste fuel storage device 3 is connected with the internal thermal reactor 5 through a force supply device 16, a solid waste conveying pipeline 12 is arranged between the solid waste fuel storage device 3 and the bottom of the dust remover 9, ash in the separator 13 is conveyed to an ash bin, and the conveying direction of solid waste in the solid waste conveying pipeline 12 is from the dust remover 9 to the solid waste fuel storage device 3; the sintering flue gas co-processing system also comprises an SNCR (selective non-catalytic reduction) denitration device 14 and an SCR denitration device 15; the SNCR denitration device 14 is arranged between the internally heated reactor 5 and the cyclone dust collector 6; the SCR denitration device is arranged at the position with the temperature of 350-400 ℃ in the rapid cooler 7.
Example 2
The embodiment provides a method for performing synergistic treatment on sintering flue gas in the steel smelting industry by using the system for performing synergistic treatment on sintering flue gas provided by embodiment 1, and the method for performing synergistic treatment comprises the steps of blowing the sintering flue gas to be treated into an internal heating type reactor 5 through a booster fan 2, blowing the sintering flue gas through a combustion fan 1 in a pulse mode, adjusting the air volume of the booster fan and the pulse parameters of the combustion fan to enable the oxygen content to be 1.8%, adjusting the internal temperature of the internal heating type reactor to be 800-1050 ℃, and enabling the flow velocity of the flue gas at the cross section of a communication pipeline between the internal heating type reactor 5 and a cyclone dust collector 6 to be 25 m/s. And finally, the solid waste generated by the dust remover 9 is conveyed back to the solid waste fuel storage device 3 through the solid waste conveying pipeline 12 and then enters the internal heating type reactor 5 for secondary treatment, and the treated solid waste is converted into stable solid ash. Flue gas disturbance is carried out by utilizing combustion-supporting air in the internal heating type reactor 5, the speed of the combustion-supporting fan (1) blowing into the reactor is controlled by adjusting a valve of a combustion-supporting air pipeline (4), irregular pulse airflow is formed, flue gas in the reactor is disturbed, the retention time of the flue gas in the reactor is ensured to be more than 3 seconds, and the carbon monoxide and the dioxin are ensured to be treated completely.
Example 3
The embodiment provides a method for performing synergistic treatment on sintering flue gas in the steel smelting industry by using the system for performing synergistic treatment on sintering flue gas provided by embodiment 1, wherein the method for performing synergistic treatment on the sintering flue gas comprises the steps of blowing the sintering flue gas to be treated into an internal heating type reactor 5 through a booster fan 2, blowing the sintering flue gas through a combustion fan 1 in a pulse mode, adjusting the air quantity of the booster fan and the pulse parameters of the combustion fan to enable the oxygen content to be 1.0%, the internal temperature of the internal heating type reactor to be 800-1050 ℃, enabling the sintering flue gas to flow along a flue gas conveying pipeline after being combusted in the internal heating type reactor 5, and enabling the cross-section flue gas flow velocity of a communicating pipeline between the internal heating type reactor 5 and a cyclone dust collector 6 to be 20 m/s. And finally, the solid waste generated by the dust remover 9 is conveyed back to the solid waste fuel storage device 3 through the solid waste conveying pipeline 12 and then enters the internal heating type reactor 5 for secondary treatment, and the treated solid waste is converted into stable solid ash.
Example 4
The embodiment provides a method for performing synergistic treatment on sintering flue gas in the steel smelting industry by using the system for performing synergistic treatment on sintering flue gas provided by embodiment 1, wherein the method for performing synergistic treatment on the sintering flue gas comprises the steps of blowing the sintering flue gas to be treated into an internal heating type reactor 5 through a booster fan 2, blowing the sintering flue gas through a combustion fan 1 in a pulse mode, adjusting the air quantity of the booster fan and the pulse parameters of the combustion fan to enable the oxygen content to be 0.5%, the internal temperature of the internal heating type reactor to be 800-1050 ℃, enabling the sintering flue gas to flow along a flue gas conveying pipeline after being combusted in the internal heating type reactor 5, and enabling the cross-section flue gas flow velocity of a communicating pipeline between the internal heating type reactor 5 and a cyclone dust collector 6 to be 30 m/s. And finally, the solid waste generated by the dust remover 9 is conveyed back to the solid waste fuel storage device 3 through the solid waste conveying pipeline 12 and then enters the internal heating type reactor 5 for secondary treatment, and the treated solid waste is converted into stable solid ash.
Comparative example 1
The comparative example provides a method for carrying out synergistic treatment on sintering flue gas in the steel smelting industry, and the method is only different from the embodiment 2 in that dioxin in the flue gas cannot be decomposed and removed when the temperature in the internal heating type reactor 5 is less than 800 ℃ and the temperature is less than 800 ℃, and the SNCR denitration reduction reaction cannot be carried out at the same time, so that the denitration efficiency is low, and the cost is increased.
Comparative example 2
The comparative example provides a method for carrying out synergistic treatment on sintering flue gas in the steel smelting industry, and only the difference from the example 2 is that the temperature in the internal heating type reactor 5 is higher than 1050 ℃, the whole size and investment of equipment are increased under the condition, the requirement on heat-insulating materials is greatly improved, thermal nitrogen oxides are generated in the reactor when the temperature is higher than 1050 ℃, the denitration cost is increased, and the denitration efficiency is reduced.
Comparative example 3
The comparative example provides a method for carrying out synergistic treatment on sintering flue gas in the steel smelting industry, and the method is only different from the method in the example 2 in that the oxygen content in the reactor 5 is adjusted to be 6%, in this case, nitrogen oxide is secondarily produced in the internal heating type reactor 5, and the denitration load denitration efficiency is increased.
Comparative example 4
The comparative example provides a method for performing synergistic treatment on sintering flue gas in the steel smelting industry, and the method is only different from the embodiment 2 in that a solid waste conveying pipeline 12 is arranged in the synergistic treatment system for sintering flue gas, and the finally obtained solid waste contains 55% of calcium sulfite by mass.
The denitration efficiency, desulfurization efficiency, dioxin removal rate, carbon monoxide removal rate and secondary pollutant emission results of the above examples 2 to 4 are shown in table 1.
Table 1 comparative table of sintering fume treatment results of examples 2 to 4
It should be noted that, in the case of conflict, the features in the embodiments of the present invention may be combined with each other.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. A sintering flue gas cooperative processing system comprises a flue gas conveying pipeline and equipment connected in series by the flue gas conveying pipeline, and is characterized in that the equipment sequentially comprises an internal heating type reactor (5), a cyclone dust collector (6), a rapid cooler (7), a desulfurizing tower (8), a dust collector (9), an induced draft fan (11) and a gas external exhaust device according to the flue gas conveying direction; a separator (13) is arranged at the bottom of the desulfurizing tower (8); at least one solid waste conveying pipeline (12) is arranged between the devices, and the solid waste conveying direction in the solid waste conveying pipeline (12) is opposite to the flue gas conveying direction; the bottom of the internal heating type reactor (5) is provided with a booster fan (2) and a combustion-supporting air pipeline (4), and the combustion-supporting air pipeline (4) is connected with a combustion-supporting fan (1); an SNCR denitration device (14) is arranged between the internal heating type reactor (5) and the cyclone dust collector (6); an SCR denitration device (15) is arranged in the rapid cooler (7); the internal heating type reactor (5) is also connected with a fuel supply device.
2. The synergistic sintering flue gas treatment system as claimed in claim 1, wherein the gas discharge device comprises an atmospheric air discharge device.
3. The synergistic treatment system for sintering flue gas as recited in claim 2, wherein the gas discharge device comprises a chimney (10).
4. The synergistic treatment system for the sintering flue gas as claimed in claim 1, wherein the fuel is solid waste fuel, a solid waste fuel storage device (3) is arranged upstream of the internal thermal reactor (5), and a solid waste conveying pipeline (12) is arranged between the solid waste fuel storage device (3) and the bottom of the dust remover (9).
5. The system for co-processing sintering flue gas as recited in claim 4, characterized in that the solid waste fuel storage device (3) is connected with the internal thermal reactor (5) through a feeding device (16).
6. The system for the synergistic treatment of the sintering flue gas according to any one of claims 1 to 5, wherein the fuel is a combustible gas, and at least one gas combustion device is arranged on the internal thermal reactor (5).
7. The sintering flue gas co-processing system of claim 6, wherein the combustible gas comprises blast furnace gas.
8. The sintering flue gas co-processing system of claim 7, wherein the blast furnace gas comprises steel plant blast furnace gas.
9. The sintering flue gas co-processing system according to claim 1, wherein the SCR denitration device (15) is arranged in a region with a temperature of 350-400 ℃ in the rapid cooler (7).
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