CN106984169B - Denitration system and method directly utilizing heat of sinter - Google Patents
Denitration system and method directly utilizing heat of sinter Download PDFInfo
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- B01D53/34—Chemical or biological purification of waste gases
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Abstract
The invention provides a denitration system and a denitration method directly utilizing heat of sinter, wherein the system comprises a sintering machine, cooling equipment, a waste heat recovery device, a dry desulfurization device, a dust removal device, a fan, a denitration reactor and a chimney; the flue gas outlets of the sintering machine bellows are connected with the flue gas inlets of the first and second sections of bellows, the flue gas outlets of the first and second sections of bellows are connected with the waste heat recovery device, and then are sequentially connected in series with the dry desulfurization device, the dust removal device, the booster fan and the chimney through pipelines; when the denitration reactor is a low-temperature denitration reactor, the denitration reactor is arranged between the fan and the chimney; when the denitration reactor is a medium-temperature denitration reactor, the denitration reactor is arranged between the flue gas outlets of the first section and the second section of bellows and the waste heat recovery device. The system and the method directly utilize the heat of the sintering ore, and lead the sintering flue gas to carry out low-temperature denitration reaction on the premise of not digesting extra energy consumption, thereby efficiently converting NO x The denitration rate can reach 80-90%, the embrittlement of the sintering ore can not be caused, and the waste heat of the sintering ore can be recovered.
Description
Technical Field
The invention relates to a denitration system and a denitration method, in particular to a denitration system and a denitration method directly utilizing heat of sintering ores.
Background
With the development of national economy and the increasing level of living of people, environmental problems are getting more and more attention, and nitrogen oxides (NO x ) Is always focused on by the country. According to statistics data of the environmental protection department, NO is discharged from national industrial waste gas in 2014 x 1404.8 ten thousand tons and NO discharged from ferrous metal smelting and rolling x Is one of three major sources of emissions.
The flue gas discharged by sintering machines in iron and steel enterprises (ferrous metal smelting) is the key NO x Emissions sources, their denitration, are receiving increasing attention. The ' twelve five ' plan for preventing and controlling air pollution in key areas ' clearly requires that the prevention and control of nitrogen oxide pollution be fully carried out, and the flue gas denitration demonstration of the sintering machine is actively carried out. The "action plan for preventing and treating atmospheric pollution" issued in 9 of 2013 is more required to accelerate denitration reformation in the important industry, and is believed to be important attention as the air quality in many areas is continuously bad in recent years.
The sintering machine is the largest NO in steel works x The emission source accounts for about 50% -60% of the emission of the steel plant (without the self-contained power plant), and the average emission concentration is generally 200mg/Nm 3 ～400mg/Nm 3 Also 150mg/Nm 3 ～700mg/Nm 3 In the case of (2) SO in flue gas 2 The concentration is generally 1000-3000 mg/Nm 3 The exhaust temperature of the flue gas is 100-180 ℃, and the exhaust temperature is generally difficult to meet the GB28662-2012 emission standards of atmospheric pollutants in the iron and steel sintering and pellet industry. Considering the conditions of total emission reduction, standard improvement and the like, the NO of the sintering machine x Removal has received increasing attention from owners.
At present, three main technologies are available for sintering flue gas denitration: the first method is an active carbon desulfurization and denitrification method, which can integrally remove various pollutants in flue gas, but has high equipment cost and high operation cost, and is difficult for enterprises to bear; the second is denitration by an oxidation method, NO is oxidized by an oxidant, and the existing wet desulfurization is utilized to realize the denitration purpose, and the method is not mature at present, and has the advantages of excessively high energy consumption and relatively low denitration efficiency; the third isThe SCR (Selective Catalytic Reduction) denitration of the power industry is used for denitration of the sintering flue gas, and although the SCR denitration of the power industry is very mature, the concentration of sulfur dioxide in the sintering flue gas is higher, the temperature is low and the NO is high x The concentration is low and a large amount of dust is carried, the denitration of the flue gas of the sintering machine can be directly realized without the SCR catalyst, although the temperature of the sintering flue gas can be increased to 350-450 ℃ to perform SCR denitration so as to avoid the influence of sulfur dioxide, a large amount of fuel is consumed in the mode, even if the low-temperature SCR catalyst which is mature at present is adopted, sulfur dioxide is firstly purified to a very low concentration, then the temperature is increased to be within 200 ℃ so as to perform low-temperature denitration, but the mode still needs to greatly increase the temperature of the sintering flue gas so as to reach the reaction temperature of the low-temperature SCR catalyst, and therefore, a large amount of energy is consumed by adopting the low-temperature catalyst, and the operation cost is too high.
CN 102997697A discloses a process for utilizing waste heat of sintered ore based on purification of sintered flue gas, which comprises the steps of directly exchanging heat between one part (65-85%) of flue gas after dust removal and ammonia desulfurization and sintered ore, indirectly exchanging heat between the other part (15-35%) of flue gas after final purification and emission, heating, mixing the two parts of flue gas after heating to 380 ℃, then sending the mixed flue gas into a conventional medium-temperature SCR reactor for denitration, and indirectly exchanging heat between the flue gas after denitration and the flue gas after the second part of flue gas for emission. The wet flue gas after ammonia desulfurization is directly fed into the sinter, and the wet flue gas after wet desulfurization is wet saturated flue gas and contains a plurality of liquid water, and the flue gas is directly fed into the hot sinter, so that local rapid cooling can occur to cause the sinter to be cracked, and the quality of the sinter is affected; in addition, in the technology, sintering flue gas is firstly subjected to wet desulfurization and temperature reduction, then the temperature of the flue gas is increased by utilizing the heat of the sintering ores, and in the whole process, the heat of the original sintering ores cannot be recycled through waste heat recovery, so that the energy utilization efficiency of the whole process system is low.
CN 103463946A discloses a sintering flue gas purifying method based on sintering ore catalytic action, the process directly exchanges heat between the dedusted sintering flue gas and sintering ore, and carries out selective catalytic reduction reaction under the action of sintering ore, ammonia is sprayed to convert nitrogen oxides in the flue gas into nitrogen gas, so as to achieve the effect of denitration, then the flue gas is subjected to waste heat recovery and temperature reduction to 100-150 ℃, and then is discharged from a chimney after desulfurization by an ammonia method. In the scheme, because the catalysis effect of the sinter is limited, and ammonia escape can cause serious ammonium sulfate deposition at the rear end of waste heat recovery, the ammonia spraying amount must be controlled, and only lower denitration efficiency can be realized; based on the practical condition of recycling the waste heat of the sintering ores in China, the flue gas passing through the sintering ores carries a large amount of dust and still exists after the waste heat is recycled, and the flue gas is directly sent into an ammonia desulfurization method, so that the solid balance and byproduct crystallization of a wet desulfurization system can be greatly influenced, and the long-term stable operation of the system is damaged; in addition, the temperature of the flue gas after wet desulfurization is about 50 ℃, the lifting capacity is poor, a high-floor concentration area is easy to form near a chimney, and the flue gas after domestic wet desulfurization forms a large-area flue gas plume when being discharged from the chimney at present, so that the flue gas has become a public concern.
Therefore, there is a need in the art to develop a denitration system and method that can efficiently treat sintering flue gas without digesting additional energy consumption, and that does not cause brittle fracture of the sinter and can recover the residual heat of the sinter.
Disclosure of Invention
In view of the actual needs, an object of the present invention is to provide a denitration system and a corresponding method that directly utilize heat of sinter, and the denitration system and the corresponding method can directly utilize heat of sinter, so that denitration reaction can be performed on sintering flue gas without digestion of additional energy consumption, and NO in the denitration system can be efficiently converted x The denitration rate can reach 80-90%, the embrittlement of the sintering ore can not be caused, and the waste heat of the sintering ore can be recovered.
In order to achieve the above object, in one aspect, the present invention provides a denitration system directly utilizing heat of sinter, which includes a sinter machine, sinter cooling equipment, a waste heat recovery device, a dry desulfurization device, a dust removal device, a denitration reactor and a chimney;
the sintering machine is provided with a sintering machine bellows;
the sintering ore cooling equipment is provided with a first section of air box of the cooling equipment, a second section of air box of the cooling equipment and a third section of air box of the cooling equipment along the sequence of cooling the sintering ore in the sintering ore cooling equipment, wherein a flue gas outlet of the air box of the sintering machine is connected with a flue gas inlet of the first section of air box of the cooling equipment and a flue gas inlet of the second section of air box of the cooling equipment through pipelines, the flue gas outlets of the first section of air box of the cooling equipment and the second section of air box of the cooling equipment are connected with the waste heat recovery device through pipelines, and the waste heat recovery device, the dry desulfurization device, the dust removal device, the booster fan and the chimney are sequentially connected in series through pipelines;
when the denitration reactor is a low-temperature denitration reactor, the denitration reactor is arranged on a connecting pipeline between the booster fan and the chimney, the low-temperature denitration reactor is a reactor for performing a low-temperature denitration reaction, and the low-temperature denitration reaction is performed at a temperature of less than 240 ℃ by using a low-temperature SCR denitration catalyst, for example, at 150-240 ℃;
when the denitration reactor is a medium-temperature denitration reactor, the denitration reactor is arranged on a connecting pipeline between the flue gas outlets of the first section of air box of the cooling equipment and the second section of air box of the cooling equipment and the waste heat recovery device, the medium-temperature denitration reactor is a reactor for performing medium-temperature denitration reaction, and the medium-temperature denitration reaction is performed at a temperature of more than 300 ℃, for example, at 350-420 ℃ by using a medium-temperature SCR denitration catalyst.
When the low-temperature denitration reactor is adopted in the denitration reactor, the denitration system starts from the flue gas outlets of the first section of bellows and the second section of bellows of the cooling equipment, and is sequentially connected with the waste heat recovery device, the dry desulfurization device, the dust removal device, the booster fan, the low-temperature denitration reactor and the chimney through pipelines.
When the denitration reactor is a medium-temperature denitration reactor, the denitration system starts from the flue gas outlets of the first section of bellows and the second section of bellows of the cooling equipment, and is sequentially connected with the medium-temperature denitration reactor, the waste heat recovery device, the dry desulfurization device, the dust removal device, the booster fan and the chimney through pipelines.
The low-temperature denitration reactor and the medium-temperature denitration reactor are all existing equipment, and the low-temperature SCR denitration catalyst and the medium-temperature SCR denitration catalyst adopted in the equipment are also existing catalysts, for example, the low-temperature SCR denitration catalyst can be a low-temperature vanadium-titanium-based catalyst, a low-temperature manganese-based catalyst and the like, and the low-temperature SCR denitration catalyst disclosed by CN101658787A/CN101879452A and the like is suitable for the invention. The medium-temperature SCR denitration catalyst can be a vanadium-titanium-based catalyst or other medium-high-temperature catalysts, and the like, such as the medium-temperature SCR denitration catalyst disclosed by CN102764643A/CN104209116A and the like and suitable for the invention.
The sinter cooling device is preferably a circular cooler. The annular cooler is the existing equipment, and can be generally divided into three bellows, namely a high-temperature section bellows, a medium-temperature Duan Fengxiang and a low-temperature Duan Fengxiang, which are respectively equivalent to the first bellows of the cooling equipment, the second bellows of the cooling equipment and the third bellows of the cooling equipment. After the sinter is produced from the sintering machine, the sinter is in a high-temperature state and is placed on an annular cooler, the annular cooler is provided with an annular grate layer, a plurality of cooling fans are arranged at the bottom of the annular cooler along the circumferential direction, a cover is arranged at the upper part section of the grate, and a high-temperature section bellows, a medium temperature Duan Fengxiang and a low temperature Duan Fengxiang are sequentially called from front to back.
As a specific embodiment of the denitration system of the present invention, preferably, when a low-temperature denitration reactor is adopted, fans are further disposed on connection pipes between the flue gas outlets of the first section of bellows of the cooling device and the second section of bellows of the cooling device and the waste heat recovery device;
when the medium-temperature denitration reactor is adopted, a fan is arranged on a connecting pipeline between the flue gas outlet of the first section of air box of the cooling equipment and the flue gas outlet of the second section of air box of the cooling equipment and the medium-temperature denitration reactor. The purpose of further setting up the fan is overcome system resistance, sends the flue gas into denitration reactor better and carries out denitration reaction.
As a specific embodiment of any of the foregoing denitration systems according to the present invention, preferably, the head of the sintering machine is provided with or without a dust removing device, for example, a dust removing device, which is preferably an electric dust removing device, and the dust removing device is disposed on a connection pipe between the sintering machine bellows and the first-stage bellows of the cooling apparatus and the second-stage bellows of the cooling apparatus. The electric dust remover is easy to maintain.
The sintering machine head does not need to be provided with a dust removing device, the dust removing device of the newly built sintering machine head can be omitted, and the dust removing device is concentrated to the rear end cloth bag dust remover for unified treatment, so that the system investment is reduced. In general, the existing sintering machine heads are all provided with dust removal devices, in this case, the existing sintering machine head dust removal system does not need to be modified, and the denitration system can be directly modified on the basis of the existing sintering machine head dust removal system, so that the operation flexibility of the denitration system is high.
As a specific embodiment of any one of the foregoing denitration systems of the present invention, preferably, the dry desulfurization device is a sodium-based or calcium-based rotary spray tower. The sodium-based rotary spray tower is a rotary spray tower adopting sodium carbonate as a desulfurizing agent, and the calcium-based rotary spray tower is a rotary spray tower adopting calcium oxide as a desulfurizing agent.
As a specific embodiment of any one of the foregoing denitration systems of the present invention, preferably, the dust removing device is selected from a bag-type dust remover or an electric dust remover, preferably a bag-type dust remover. Lower outlet dust concentrations can be obtained when a bag house dust collector is used.
The components included in the denitration system and the connection relation between the components ensure that the method using the denitration system can directly utilize the heat of the sintering ore, and the denitration reaction of the sintering flue gas can be carried out on the premise of not digesting extra energy consumption, so that NO in the sintering flue gas can be efficiently converted x And the method can not cause brittle fracture of the sinter and can recover the residual heat of the sinter.
On the other hand, the invention provides a denitration method directly utilizing the heat of sinter, wherein the denitration method utilizes the denitration system, the denitration method comprises the steps of introducing flue gas generated by the sinter machine into a first section of air box of cooling equipment and a second section of air box of cooling equipment after dust removal or without dust removal from the air box of the sinter machine, enabling the flue gas to directly exchange heat with sinter to be cooled in a cross flow manner, collecting the flue gas after direct heat exchange from the first section of air box of cooling equipment and the second section of air box of cooling equipment, and then sequentially discharging the flue gas after passing through the waste heat recovery device, the dry desulfurization device, the dust removal device, a booster fan, a low-temperature denitration reactor and a chimney (when the denitration reactor adopts the low-temperature denitration reactor), or
Sequentially passing through the medium-temperature denitration reactor, the waste heat recovery device, the dry desulfurization device, the dust removal device, the booster fan and the chimney and then discharging (when the medium-temperature denitration reactor is adopted by the denitration reactor).
The invention ensures that the sintering flue gas and the sintering ore to be cooled are subjected to cross-flow direct heat exchange generally means that the flue gas is directly contacted with the sintering ore from bottom to top for heat exchange when the sintering ore moves horizontally.
As a specific embodiment of the aforementioned denitration method of the present invention, it is preferable that the flue gas collected from the first stage bellows of the cooling apparatus and the second stage bellows of the cooling apparatus is directly passed through the heat recovery device to recover heat once without recycling the heat.
As a specific embodiment of the denitration method of the present invention, preferably, SO in the flue gas generated by the sintering machine 2 Not more than 3000mg/Nm 3 ，NO x Concentration of not more than 1000mg/Nm 3 Dust content of not more than 10g/Nm 3 The temperature is 80-180 ℃. In particular, the denitration method of the invention is suitable for NO in flue gas x Concentration of not more than 500mg/Nm 3 The temperature is not more than 140 ℃.
The temperature of the agglomerate to be cooled in the denitration method of the invention is generally 800-900 ℃.
As a specific embodiment of the aforementioned denitration method of the present invention, preferably, when a low-temperature denitration reactor is employed, the temperature of flue gas collected from the first stage bellows of the cooling apparatus and the second stage bellows of the cooling apparatus is controlled to be not lower than 250 ℃;
when the medium-temperature denitration reactor is adopted, the temperature of the flue gas collected from the first section of the air box of the cooling device and the second section of the air box of the cooling device is controlled to be higher than 350 ℃.
Preferably, when a low-temperature denitration reactor is adopted, the temperature of saturated steam of 0.6MPa to 0.8MPa and flue gas passing through the waste heat recovery device is not lower than 180 ℃, preferably 180 ℃ to 240 ℃.
As a specific embodiment of the denitration method of the present invention, when a low-temperature denitration reactor is used, it is preferable that the temperature of the flue gas passing through the dry desulfurization device and the dust removal device is 180 to 240 ℃, and the flue gas at the temperature is fed into the low-temperature denitration reactor.
The invention mainly provides a denitration system and a corresponding method for directly utilizing the heat of sintering ores, and the denitration system and the corresponding method can enable sintering flue gas to carry out denitration reaction on the premise of not digesting extra energy consumption and efficiently convert NO in the sintering flue gas x The denitration rate can reach 80-90%, the embrittlement of the sinter is avoided, the waste heat of the sinter can be recovered, and the method has the following advantages:
(1) The dust removal of the head of the newly built sintering machine can be omitted, and the dust is concentrated to the rear-end bag-type dust remover for unified treatment, so that the system investment is reduced; the existing sintering machine head dust removal system does not need to be modified to reduce dust concentration, and the running operation flexibility is larger.
(2) Because the flue gas of the sintering machine is directly fed into the sintering ore cooling equipment without being cooled as a heat transfer medium, the flue gas temperature at the inlet of the waste heat recovery device at the rear end of the sintering ore cooling equipment is improved, the utilization efficiency is higher, and steam with higher pressure can be generated; the heat transfer medium for the rear end waste heat recovery device of the cooling equipment can not circulate, so that dust concentration enrichment can not occur, and the abrasion of a waste heat system and a pipeline is slowed down.
(3) The denitration efficiency of 80-90% is realized, the nitrogen oxide can reach an ultralow emission index, and the total emission reduction of a larger range can be realized.
(4) The system does not introduce a new heat source to heat the flue gas, so that the denitration temperature requirement is realized, the energy consumption is not increased, and the system operation cost is reduced.
(5) On the premise of not consuming a new heat source, the whole set of purification system has high exhaust gas temperature, effectively improves the lifting height of the exhaust gas, enhances the diffusion capacity, reduces the concentration of regional pollutants, and is beneficial to improving the quality of the regional air environment.
Drawings
FIG. 1 is a diagram of a low temperature denitration system using heat of a sintered ore directly in example 1 of the present invention.
Fig. 2 is a diagram of a medium temperature denitration system directly facilitating sintering heat in embodiment 3 of the present invention.
The reference numerals in the figures have the following meanings:
1: a sintering machine; 11: a sintering machine bellows; 2: a sinter cooling device; 21: a first section of bellows of the cooling apparatus; 22: a second section of the cooling apparatus bellows; 23: a third section of the cooling apparatus; 3: a waste heat recovery device; 4: a dry desulfurization device; 5: a dust removal device; 6: a booster fan; 7: a denitration reactor; 8: and (5) a chimney.
Detailed Description
In order to more clearly understand the technical features, objects and advantages of the present invention, the following detailed description of the technical solution of the present invention will be made with reference to specific embodiments, and it should be understood that these examples are only for illustrating the present invention and are not intended to limit the scope of the present invention. In the examples, each of the starting reagent materials is commercially available, and the experimental methods without specifying the specific conditions are conventional methods and conventional conditions well known in the art, or according to the conditions recommended by the instrument manufacturer.
Example 1
Referring to fig. 1, a diagram of a low-temperature denitration system directly utilizing heat of sinter according to the present embodiment is shown, where the low-temperature denitration system includes a sintering machine 1, a sinter cooling device 2, a waste heat recovery device 3, a dry desulfurization device 4, a dust removal device 5, a denitration reactor 7, and a chimney 8; the sintering machine is provided with a sintering machine air box 11, the sintering ore cooling equipment 2 is an existing annular cooler and is provided with a cooling equipment first section air box 21 (a high-temperature section air box), a cooling equipment second section air box 22 (a medium temperature Duan Fengxiang) and a cooling equipment third section air box 23 (a low temperature Duan Fengxiang), a flue gas outlet of the sintering machine air box 11 is connected with flue gas inlets of the cooling equipment first section air box 21 and the cooling equipment second section air box 22 after being split through pipelines, the flue gas outlets of the cooling equipment first section air box 21 and the cooling equipment second section air box 22 are connected with the waste heat recovery device 3 through pipelines after being collected, and the waste heat recovery device 3, the dry desulfurization device 4, the dust removal device 5, the booster fan 6, the denitration reactor 7 and the chimney 8 are sequentially connected in series through pipelines;
the denitration reactor 7 in this embodiment is a low-temperature denitration reactor, and the low-temperature denitration reactor 7 is a reactor for performing a low-temperature denitration reaction, and the low-temperature denitration reaction is performed at 150 to 240 ℃ by using a low-temperature SCR denitration catalyst.
The low-temperature SCR denitration catalyst adopted in the embodiment is a low-temperature vanadium-titanium-based catalyst or a low-temperature manganese-based/iron-based catalyst, and can be obtained by performing a low-temperature denitration SCR reaction at 150-240 ℃.
The low-temperature denitration reaction system of the embodiment is a newly-built sintering machine head, and a machine head dust removing device of the sintering machine 1 is omitted.
The dry desulfurization device used in this example is a sodium-based rotary spray tower. The desulfurizing agent adopted by the sodium-based rotary spray tower is a rotary spray tower of sodium carbonate.
The dust removing device adopted in the embodiment is a bag-type dust remover.
The specific low-temperature denitration method comprises the following steps:
the flue gas from the newly built sintering machine bellows 11 is collected together, and SO in the sintering flue gas 2 The concentration is 1000mg/Nm 3 ，NO x The concentration was 400mg/Nm 3 Dust content of 3000mg/Nm 3 The temperature of the flue gas is 120 ℃, the sintering flue gas is directly introduced into the sintering ore cooling equipment 2, and is subjected to cross flow direct heat exchange with the sintering ore at 800-900 ℃ in the sintering ore cooling equipment 2, the flue gas after heat exchange is collected from the first section of air box 21 of the cooling equipment and the second section of air box 22 of the cooling equipment, the temperature of the flue gas reaches 450 ℃, and the dust content of the flue gas is reduced to 900mg/Nm after the flue gas passes through a sintering ore deposit layer on the sintering ore cooling equipment 2 3 Introducing the flue gas into a waste heat recovery device 3 to directly generate 0.6MPa saturated steam, recycling heat, reducing the temperature of the flue gas to 200 ℃, introducing the flue gas into a dry desulfurization tower 4 (a sodium-based rotary spray tower) for desulfurization, and then dedusting by a dedusting device 5 (a cloth bag dust remover), wherein SO in the flue gas is removed at the moment 2 At a concentration of 10mg/Nm 3 ，NO x The concentration was 400mg/Nm 3 Dust content of 10mg/Nm 3 The flue gas temperature is 180 ℃, the system resistance is overcome by a booster fan 6, the flue gas is blown into a low-temperature denitration reactor 7, and NO is generated x Down to 80mg/Nm 3 The denitration rate is 80%, the temperature of the flue gas is 165 ℃, and the flue gas is directly sent into a chimney 8 for discharge.
Example 2
The low-temperature denitration system adopted in this embodiment is basically the same as that in embodiment 1, except that this embodiment is an existing sintering machine, which is itself provided with a sintering machine dust removing device (not shown in the figure), and the dust removing device is an electric dust removing device which is disposed on the connection pipe between the sintering machine bellows 11 and the first-stage bellows 21 of the cooling apparatus and the second-stage bellows of the cooling apparatus.
The flue gases led out from the existing sintering machine bellows 11 are gathered together, and SO in the flue gases is contained in the flue gases 2 At a concentration of 2000mg/Nm 3 ，NO x The concentration was 500mg/Nm 3 Dust content of 2000mg/Nm 3 The temperature of the flue gas is 140 ℃, the sintering flue gas is subjected to an electric dust removing device, and the dust content is reduced to 150mg/Nm 3 Then the mixture is introduced into a sinter cooling device 2, heat exchange is directly carried out on the mixture and the sinter at 800-900 ℃ in the sinter cooling device 2 in a cross flow manner, the flue gas after the heat exchange is collected from a first section of bellows 21 of the cooling device and a second section of bellows 22 of the cooling device, the temperature of the flue gas reaches 500 ℃, and the dust content of the flue gas is increased to 400mg/Nm after the flue gas passes through a sinter deposit layer on the sinter cooling device 2 3 Introducing the flue gas into a waste heat recovery device 3 to directly generate 0.8MPa saturated steam, recycling heat, reducing the temperature of the flue gas to 240 ℃, introducing the flue gas into a dry desulfurization device 4 (sodium-based rotary spray) tower for desulfurization, and then dedusting by a dedusting device (cloth bag deduster), wherein SO in the flue gas is removed at the moment 2 At a concentration of 10mg/Nm 3 ，NO x The concentration was 500mg/Nm 3 Dust content of 10mg/Nm 3 The flue gas temperature is 190 ℃, the system resistance is overcome by the booster fan 6, the flue gas is blown into the low-temperature denitration reactor 7, and NO is generated x Down to 50mg/Nm 3 The denitration rate is 90 percent, the temperature of the flue gas is 170 ℃, and the flue gas is directly sent into a chimney 8 for discharge.
Example 3
Referring to fig. 2, a diagram of a medium-temperature denitration system directly utilizing heat of a sinter according to the present embodiment is shown, where the medium-temperature denitration system includes a sintering machine 1, a sinter cooling device 2, a waste heat recovery device 3, a dry desulfurization device 4, a dust removal device 5, a medium-temperature denitration reactor 7, and a chimney 8; the sintering machine is provided with a sintering machine air box 11, the sintering ore cooling equipment 2 is an existing annular cooler, the sintering machine is provided with a cooling equipment first section air box 21 (a high temperature section air box), a cooling equipment second section air box 22 (a medium temperature Duan Fengxiang) and a cooling equipment third section air box 23 (a low temperature Duan Fengxiang), a flue gas outlet of the sintering machine air box 11 is connected with flue gas inlets of the cooling equipment first section air box 21 and the cooling equipment second section air box 22 after being split through pipelines, the flue gas outlets of the cooling equipment first section air box 21 and the cooling equipment second section air box 22 are connected with the medium temperature denitration reactor 7 through pipelines after being collected, and the medium temperature denitration reactor 7, the waste heat recovery device 3, the dry desulfurization device 4, the dust removal device 5, the booster fan 6 and the chimney 8 are sequentially connected in series through pipelines;
the medium-temperature denitration reactor 7 is a reactor for performing a medium-temperature denitration reaction, and the medium-temperature denitration reaction is performed at 300 ℃ or higher by using a medium-temperature SCR denitration catalyst.
The medium-temperature SCR denitration catalyst adopted in the embodiment is a conventional medium-temperature vanadium-titanium-based catalyst, can perform a low-temperature denitration SCR reaction at 350-420 ℃, and can be obtained commercially.
The flue gas from the newly built sintering machine bellows 11 is collected together, and SO in the sintering flue gas 2 The concentration was 1500mg/Nm 3 ，NO x The concentration was 500mg/Nm 3 Dust content of 4000mg/Nm 3 The temperature of the flue gas is 110 ℃, the sintering flue gas is directly introduced into the sintering ore cooling equipment 2, and is subjected to cross flow direct heat exchange with the sintering ore at 800-900 ℃ in the sintering ore cooling equipment 2, the flue gas after heat exchange is collected from the first section of air box 21 of the cooling equipment and the second section of air box 22 of the cooling equipment, the temperature of the flue gas reaches 430 ℃, and the dust content of the flue gas is reduced to 1000mg/Nm after the flue gas passes through a sintering ore deposit layer on the sintering ore cooling equipment 2 3 Introducing the flue gas into a medium-temperature denitration reactor 7, and carrying out denitration to obtain NO x The concentration was 50mg/Nm 3 The denitration efficiency is 90%, the temperature is 415 ℃, other parameters are unchanged, then the flue gas enters the waste heat recovery device 3 to directly generate 0.6MPa saturated steam, heat is not recycled, the temperature of the flue gas is reduced to 150 ℃,the flue gas enters a dry desulfurization tower 4 (sodium-based or calcium-based rotary spray tower) for desulfurization, and then is subjected to dust removal by a dust removal device 5 (a bag-type dust remover), and SO in the flue gas is removed at the moment 2 The concentration was 100mg/Nm 3 ，NO x The concentration was 50mg/Nm 3 Dust content of 10mg/Nm 3 The temperature of the flue gas is 95 ℃, and the flue gas is directly sent into a chimney 8 for discharge after overcoming the system resistance through a booster fan 6.
The last explanation is: the above embodiments are only for illustrating the implementation procedure and features of the present invention, and not for limiting the technical solution of the present invention, and although the present invention has been described in detail with reference to the above embodiments, it should be understood by those of ordinary skill in the art that: modifications and equivalents may be made thereto without departing from the spirit and scope of the invention, and any modifications and equivalents are intended to be included within the scope of the present invention.
Claims (16)
1. The denitration system directly utilizing the heat of the sinter comprises a sinter machine (1), sinter cooling equipment (2), a waste heat recovery device (3), a dry desulfurization device (4), a dust removal device (5), a booster fan (6), a denitration reactor (7) and a chimney (8);
the sintering machine (1) is provided with a sintering machine bellows (11);
the sinter cooling device (2) is an annular cooler, and the dry desulfurization device (4) is a sodium-based or calcium-based rotary spray tower;
the sintering ore cooling device (2) is sequentially provided with a first section of air box (21) of the cooling device, a second section of air box (22) of the cooling device and a third section of air box (23) of the cooling device along the sequence of cooling the sintering ore to be cooled in the sintering ore cooling device (2), the flue gas outlets of the air box (11) of the sintering machine are connected with the flue gas inlets of the first section of air box (21) of the cooling device and the second section of air box (22) of the cooling device through pipelines, the flue gas outlets of the first section of air box (21) of the cooling device and the second section of air box (22) of the cooling device are connected with the waste heat recovery device (3) through pipelines, and the waste heat recovery device (3), the dry desulfurization device (4), the dust removal device (5), the booster fan (6) and the chimney (8) are sequentially connected in series through pipelines;
when the denitration reactor (7) is a low-temperature denitration reactor, the denitration reactor is arranged on a connecting pipeline between the booster fan (6) and the chimney (8), the low-temperature denitration reactor is a reactor for performing a low-temperature denitration reaction, and the low-temperature denitration reaction utilizes a low-temperature SCR denitration catalyst at a temperature of not more than 240 DEG C o C, performing;
when the denitration reactor (7) is a medium-temperature denitration reactor, the denitration reactor is arranged on a connecting pipeline between a flue gas outlet of the first section of air box (21) of the cooling equipment and the second section of air box (22) of the cooling equipment and the waste heat recovery device (3), the medium-temperature denitration reactor is a reactor for performing medium-temperature denitration reaction, and the medium-temperature denitration reaction is performed at a temperature of above 300 ℃ by using a medium-temperature SCR denitration catalyst.
2. The denitration system using directly sinter heat according to claim 1, wherein:
when the low-temperature denitration reactor is adopted, a fan is also arranged on a connecting pipeline between a flue gas outlet of the first section of air box (21) of the cooling equipment and the second section of air box (22) of the cooling equipment and the waste heat recovery device (3);
when the medium-temperature denitration reactor is adopted, a fan is further arranged on a connecting pipeline between the flue gas outlet of the first section of air box (21) of the cooling equipment and the flue gas outlet of the second section of air box (22) of the cooling equipment and the medium-temperature denitration reactor.
3. The denitration system directly utilizing the heat of the sintering ore according to claim 1, wherein the head of the sintering machine is provided with or without a dust removing device, such as a dust removing device, and the dust removing device is arranged on a connecting pipeline of the sintering machine bellows (11) and the first-section bellows (21) and the second-section bellows (22) of the cooling equipment.
4. The denitration system directly utilizing sintering ore heat according to any one of claims 1-3, wherein the dust removing device (5) is a bag-type dust remover or an electric dust remover.
5. The denitration system directly utilizing the heat of the sinter as claimed in claim 4, wherein the dust removing device (5) is a bag-type dust remover.
6. The denitration system directly utilizing sintering ore heat according to claim 1, wherein the low-temperature denitration reaction utilizes a low-temperature SCR denitration catalyst in a range of 150-240 DEG o C.
7. A denitration system directly utilizing heat of sintered ore according to claim 3, wherein the dust removing device is an electric dust removing device.
8. The denitration system directly utilizing sintering ore heat according to claim 1, wherein the medium-temperature denitration reaction utilizes a medium-temperature SCR denitration catalyst at a temperature of 350-420 DEG C o C.
9. A denitration method directly utilizing sinter heat, wherein the denitration method utilizes the denitration system directly utilizing sinter heat as claimed in any one of claims 1-8, the denitration method comprises the steps of introducing flue gas generated by a sintering machine (1) into a first section of air box (21) of cooling equipment and a second section of air box (22) of cooling equipment after dust removal or without dust removal from an air box (11) of the sintering machine, enabling the flue gas to directly exchange heat with sinter to be cooled in a cross flow manner, collecting the flue gas after direct heat exchange from the first section of air box (21) of the cooling equipment and the second section of air box (22) of the cooling equipment, and then sequentially passing through a waste heat recovery device (3), a desulfurization device (4), a dust removal device (5), a booster fan (6), a low-temperature denitration reactor and a chimney (8) for discharge, or dry method
Sequentially passes through a medium-temperature denitration device, a waste heat recovery device (3), a dry desulfurization device (4), a dust removal device (5), a booster fan (6) and a chimney (8) and is discharged.
10. The denitration method using directly the heat of sintered ore according to claim 9, wherein the flue gas collected from the first stage windbox of the cooling apparatus and the second stage windbox of the cooling apparatus is directly passed through the heat recovery device to recover the heat once without recycling the heat.
11. The denitration method by directly utilizing heat of sintering ore according to claim 9, wherein SO in flue gas generated by the sintering machine 2 The concentration of (2) is not more than 3000 mg-Nm 3 ，NO x The concentration is not more than 1000 mg%Nm 3 Dust is not more than 10 g-Nm 3 The temperature is 80-180 DEG o C。
12. The denitration method by directly utilizing heat of sintered ore as claimed in claim 11, wherein NO in the flue gas x The concentration is not more than 500 mg%Nm 3 At a temperature of not more than 140 o C。
13. The denitration method using directly the heat of sintered ore according to claim 11, wherein:
when the low-temperature denitration reactor is adopted, the temperature of the flue gas collected from the first section of the air box of the cooling equipment and the second section of the air box of the cooling equipment is controlled to be not lower than 250 o C；
When the medium-temperature denitration reactor is adopted, the temperature of the flue gas collected from the first section of the air box of the cooling equipment and the second section of the air box of the cooling equipment is controlled to be not lower than 350 o C。
14. The method according to claim 13, wherein when the low-temperature denitration reactor is used, the waste heat recovery device generates saturated steam of 0.6MPa to 0.8MPa and the temperature of the flue gas passing through the waste heat recovery device is not lower than 180 ℃ o C。
15. The denitration method by directly utilizing heat of sinter as claimed in claim 14, wherein the temperature of flue gas passing through the waste heat recovery device is 180-240 ℃ o C。
16. The method for direct use of sinter heat according to claim 13, wherein when a low-temperature denitration reactor is used, the flue gas temperature passing through the dry desulfurization device and the dust removal device is 180 to 240 o And C, sending the flue gas with the temperature into the low-temperature denitration reactor.
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| CN111678350A (en) * | 2020-06-03 | 2020-09-18 | 首钢集团有限公司 | Sintering flue gas cooling sinter system |
| CN115055036A (en) * | 2022-07-18 | 2022-09-16 | 北京中冶设备研究设计总院有限公司 | From denitration system |
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