CN215276478U - Sintering flue gas multi-pollutant ultralow emission system - Google Patents
Sintering flue gas multi-pollutant ultralow emission system Download PDFInfo
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- CN215276478U CN215276478U CN202120996396.5U CN202120996396U CN215276478U CN 215276478 U CN215276478 U CN 215276478U CN 202120996396 U CN202120996396 U CN 202120996396U CN 215276478 U CN215276478 U CN 215276478U
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Abstract
The utility model discloses an ultralow discharge system of sintering flue gas multi-pollutant, include electrostatic precipitator, compensation heating device, denitrification facility and the desulphurization unit that set gradually along the flue gas flow direction, the electrostatic precipitator entry end the desulphurization unit exit end sets up first heat exchanger group, first heat exchanger group will the high temperature flue gas of electrostatic precipitator entry end with the low temperature flue gas of desulphurization unit exit end carries out the heat transfer. The first heat exchanger groups are arranged at the inlet end of the electric dust remover and the outlet end of the desulphurization device, so that the flue gas is subjected to heat exchange and cooling before entering the electric dust remover, the phenomenon that the specific resistance in the electric dust remover is increased due to overhigh flue gas temperature is avoided, and the dust removal efficiency is reduced; the high temperature of the flue gas heats up the flue gas at the outlet of the desulfurization device under the action of the first heat exchanger group, so that the diffusion of the flue gas is facilitated, and the problem that the flue gas generates smoke plume due to water vapor condensation at the discharge position is avoided.
Description
Technical Field
The utility model relates to a steel flue gas environmental protection technical field especially relates to an ultralow discharge system of many pollutants of sintering flue gas.
Background
China is the largest steel producing country in the world, the yield of crude steel in 2018 is 9.28 hundred million tons, which accounts for 51.3 percent of the total yield of crude steel in the world, the treatment levels of pollutants in the steel industry are different, and the steel industry exceeds the power industry and becomes the most main air pollutant emission source of the industrial department. Wherein, sintering is the process with the largest pollutant emission in the whole steel process, and SO emitted by sintering flue gas is counted2NOx and PM respectively account for more than 85%, 60% and 40% of the total pollutant emission amount of the whole process of steel production, so that the sintering flue gas can be discharged after dust removal, denitration and desulfurization treatment.
The application numbers are: 201610857619.3, the invention discloses a system for simultaneously desulfurizing and denitrating sintered flue gas and a realization method thereof, wherein high-temperature sintered ore is used for heating the flue gas entering a denitrating device, a waste heat boiler is arranged for exchanging heat with the high-temperature flue gas to cool the flue gas entering the desulfurizing device, and meanwhile, a part of steam generated by the waste heat boiler heats the desulfurized flue gas to eliminate the phenomena of white smoke, tailing, chimney rain and the like of the flue gas. However, the utilization rate of the whole process of the self heat of the flue gas in the patent is not sufficient, and needs to be further improved.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing an ultralow discharge system of many pollutants of sintering flue gas to solve the problem that above-mentioned prior art exists, through setting up a set of heat transfer device at electrostatic precipitator entry end and desulphurization unit exit end, utilize flue gas self heat to rise the flue gas temperature of desulphurization unit exit end and reduced the flue gas temperature of electrostatic precipitator entry end in, improved flue gas self heat's utilization ratio, thereby further improve flue gas pollutants's desorption efficiency.
In order to achieve the above object, the utility model provides a following scheme: the utility model provides an ultralow discharge system of sintering flue gas multi-pollutant, include electrostatic precipitator, compensation heating device, denitrification facility and the desulphurization unit that set gradually along the flue gas flow direction, the electrostatic precipitator entry end the desulphurization unit exit end sets up first heat exchanger group, first heat exchanger group will the high temperature flue gas of electrostatic precipitator entry end with the low temperature flue gas of desulphurization unit exit end carries out the heat transfer.
Preferably, the first heat exchanger group is in including setting up the one-level heat exchanger of electrostatic precipitator entry end and setting are in the second grade heat exchanger of desulphurization unit exit end, the one-level heat exchanger with the second grade heat exchanger intercommunication, just the one-level heat exchanger with heat transfer medium circulation heat transfer in the second grade heat exchanger.
Preferably, the inlet end of the compensation heating device and the outlet end of the denitration device are provided with a second heat exchanger set, and the second heat exchanger set exchanges heat between the low-temperature flue gas at the inlet end of the compensation heating device and the high-temperature flue gas at the outlet end of the denitration device.
Preferably, the second heat exchanger group is a rotary gas-gas heat exchanger.
Preferably, a particle conditioning device for conditioning the flue gas is further arranged between the outlet end of the second heat exchanger group and the inlet end of the compensation heating device.
Preferably, the granule quenching and tempering device includes venturi tube, venturi tube's entry section with the exit end of second heat exchanger group links to each other, venturi tube's diffuser segment with the offset heating device entry end links to each other, venturi tube's throat links to each other with the container that contains alkaline powder.
Preferably, the inlet end of the electric dust collector, the inlet end of the compensation heating device and the inlet end of the denitration device are all provided with temperature sensors.
Another object of the present invention is to provide an operation temperature control method, comprising the steps of,
1) raw flue gas enters a first heat exchanger group to exchange heat with heat exchange media in the first heat exchanger group, and the temperature of the raw flue gas is reduced to obtain low-temperature flue gas;
2) after the low-temperature flue gas is dedusted by the electric deduster, the low-temperature flue gas enters a second heat exchanger group for heat exchange, and the temperature of the flue gas is raised;
3) the heated flue gas is further heated by a compensation heating device to reach a temperature range required by the denitration reaction;
4) high-temperature flue gas flowing out of the denitration device enters the second heat exchanger group for heat exchange, the temperature of the flue gas is reduced, and the flue gas with the reduced temperature enters the desulfurization device for desulfurization reaction to obtain low-temperature clean flue gas;
5) and the low-temperature clean flue gas enters the first heat exchanger group to exchange heat with the heat exchange medium, the temperature of the low-temperature clean flue gas is increased, and the low-temperature clean flue gas is discharged into the air.
Preferably, in step 3), a flue gas temperature threshold of an inlet end of the compensation heating device is preset according to the temperature required by the inlet end of the denitration device, and when the detected flue gas temperature of the inlet end of the compensation heating device is lower than the flue gas temperature threshold of the inlet end of the compensation heating device, the compensation heating device is started, a compensation heating value of the compensation heating device is adjusted according to the temperature difference, and the flue gas temperature value required by the inlet end of the denitration device is ensured.
Preferably, on the basis of guaranteeing the required flue gas temperature value of denitrification facility entry end, adjust the heat transfer capacity of first heat exchanger group reduces the flue gas temperature of electrostatic precipitator entry end.
The utility model discloses for prior art gain following technological effect:
1. the first heat exchanger groups are arranged at the inlet end of the electric dust remover and the outlet end of the desulphurization device, so that the flue gas is subjected to heat exchange and cooling before entering the electric dust remover, the phenomenon that the specific resistance in the electric dust remover is increased due to overhigh flue gas temperature is avoided, and the dust removal efficiency is reduced; the high temperature of the flue gas heats up the flue gas at the outlet of the desulfurization device under the action of the first heat exchanger group, so that the diffusion of the flue gas is facilitated, and the problem that the flue gas generates smoke plume due to water vapor condensation at the discharge position is avoided.
2. Through setting up second heat exchanger group at offset heating device entry end and denitrification facility exit end for the low temperature flue gas that flows from electrostatic precipitator carries out preliminary intensification through the heat exchange of the inside flue gas self of system at first before through offset heating device, thereby reduces offset heating device's energy consumption, and simultaneously, the high temperature flue gas that flows from denitrification facility gets into second heat exchanger group and carries out the heat transfer after, the temperature reduces, the flue gas that has still guaranteed to get into desulphurization unit has lower temperature.
3. The particle conditioning device for conditioning the flue gas is arranged between the outlet end of the second heat exchanger group and the inlet end of the compensation heating device, so that the viscosity of the fly ash in the flue gas is adjusted, and the situation that the pressure drop is increased due to the blockage of a catalyst pore channel in the denitration device caused by the high viscosity of the fly ash in the flue gas is avoided.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive labor.
FIG. 1 is a schematic diagram of the overall structure of a sintering flue gas multi-pollutant ultra-low emission system;
FIG. 2 is a flow chart of operating temperature control;
wherein, 1, a first-stage heat exchanger; 2. an electric dust collector; 3. a rotary gas-gas heat exchanger; 4. a particle conditioning device; 5. a compensation heating device; 6. a denitration device; 7. a desulfurization unit; 8. a secondary heat exchanger; q1Raw flue gas; q2And purifying the smoke.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The utility model aims at providing an ultralow discharge system of many pollutants of sintering flue gas to solve the problem that prior art exists, through setting up a set of heat transfer device at electrostatic precipitator entry end and desulphurization unit exit end, utilize flue gas self heat to rise the flue gas temperature of desulphurization unit exit end and reduced the flue gas temperature of electrostatic precipitator entry end in the time, improved flue gas self thermal utilization ratio, thereby further improve the desorption efficiency of flue gas pollutant.
In order to make the above objects, features and advantages of the present invention more comprehensible, the present invention is described in detail with reference to the accompanying drawings and the detailed description.
Please refer to fig. 1-2.
Example one
The embodiment provides a sintering flue gas multi-pollutant ultra-low emission system, which comprises an electric dust collector 2, a compensation heating device 5, a denitration device 6 and a desulfurization device 7 which are sequentially arranged along the flow direction of flue gas, wherein the compensation heating device 5 can adopt any device capable of heating up and heating the flue gas flowing through the compensation heating device, such as an electric heating device, a fuel gas heating device and the like, a wet desulfurization process is adopted in the desulfurization device 7, and the desulfurization device 7 can be a wet desulfurization tower or other devices capable of performing wet desulfurization; the inlet end of the electric dust collector 2 and the outlet end of the desulphurization device 7 are provided with first heat exchanger groups, and the first heat exchanger groups exchange heat between high-temperature flue gas at the inlet end of the electric dust collector 2 and low-temperature flue gas at the outlet end of the desulphurization device 7, so that the flue gas is cooled by heat exchange before entering the electric dust collector 2, and the phenomenon that the specific resistance in the electric dust collector 2 is increased due to overhigh flue gas temperature is avoided, so that the spark voltage is reduced, and the dust removal efficiency is reduced; the high temperature of the flue gas heats up the flue gas at the outlet of the desulfurization device 7 under the action of the first heat exchanger group, so that the diffusion of the flue gas is facilitated, and the problem that the flue gas generates smoke plume due to water vapor condensation at the discharge position is avoided.
When the first heat exchanger group comprises two heat exchangers, a heat exchange medium between the two heat exchangers needs to circulate, so that heat exchange is carried out on the flue gas at two different temperatures; in this embodiment, the first heat exchanger group comprises a first heat exchanger 1 arranged at the inlet end of the electric dust collector 2 and a second heat exchanger 8 arranged at the outlet end of the desulphurization device 7, the first heat exchanger 1 is communicated with the second heat exchanger 8, and the first heat exchanger 1 and a heat exchange medium in the second heat exchanger 8 perform circulating heat exchange; wherein first order heat exchanger 1 and second grade heat exchanger 8 preferably adopt the heat exchanger of the same type, in this embodiment, select tube bundle heat exchanger for use, use water as heat transfer medium to carry out the heat transfer to the flue gas of two different temperatures.
Further, a second heat exchanger group is arranged at the inlet end of the compensation heating device 5 and the outlet end of the denitration device 6, and the second heat exchanger group exchanges heat between the low-temperature flue gas at the inlet end of the compensation heating device 5 and the high-temperature flue gas at the outlet end of the denitration device 6; the temperature of the flue gas flowing out of the electric dust collector 2 is low, heat exchange is carried out after the flue gas passes through the second heat exchanger group, the temperature is increased, namely, before the flue gas is heated through the compensation heating device 5, the flue gas is primarily heated through the self heat exchange of the flue gas in the system, and therefore the energy consumption of the compensation heating device 5 is reduced; meanwhile, after the high-temperature flue gas flowing out of the denitration device 6 enters the second heat exchanger group for heat exchange, the temperature is reduced, so that the flue gas entering the desulfurization device 7 is ensured to have lower temperature.
When the second heat exchanger group comprises two heat exchangers, a heat exchange medium between the two heat exchangers needs to circulate, so that heat exchange is carried out on the flue gas at two different temperatures; in this embodiment, the second heat exchanger group adopts a heat exchanger, and for rotation type gas heat exchanger 3, rotation type gas heat exchanger 3's heat exchange efficiency is high, is favorable to improving the thermal utilization ratio of flue gas self.
In this embodiment, a process of adding a catalyst to perform denitration is preferably adopted in the denitration device 6, so as to further improve the denitration process on NO in the flue gasXThe particle conditioning device 4 for conditioning the flue gas is further arranged between the outlet end of the second heat exchanger group and the inlet end of the compensating heating device 5, the viscosity of the fly ash in the flue gas is adjusted through the particle conditioning device 4, and the situation that the pressure drop is increased due to the blockage of a catalyst pore channel in the denitration device 6 caused by the high viscosity of the fly ash in the flue gas is avoided.
Further, the particle conditioning device 4 comprises a venturi tube, the inlet section of the venturi tube is connected with the outlet end of the second heat exchanger group, the diffusion section of the venturi tube is connected with the inlet end of the compensation heating device 5, and when the flue gas flows through the venturi tube, negative pressure is formed at the throat part; wherein venturi can set up one and also can set up a plurality ofly, when flue cross-section diameter between second heat exchanger group and compensation heating device 5 is great, can be along a plurality of venturi of flue cross-section evenly distributed in the flue to make flue gas can with the more abundant mixture of alkaline powder, a plurality of venturi pass through the grid frame to be fixed in the flue.
Furthermore, the compensation heating device 5 is a gas compensation heater, the gas compensation heater can directly mix high-temperature gas generated after gas combustion with flue gas, so that the temperature of the flue gas is increased, and meanwhile, the gas compensation heater can adjust the flow of the gas through a valve to ensure that the flue gas is heated to an optimal temperature range suitable for denitration reaction.
Further, 2 entry ends of electrostatic precipitator, 5 entry ends of compensation heating device, 6 entry ends of denitrification facility all are provided with temperature sensor, through the real-time supervision of temperature sensor to relevant position flue gas to guarantee entire system's high-efficient operation.
Example two
The embodiment provides an operation temperature control method, which is applied to the sintering flue gas multi-pollutant ultra-low emission system in the first embodiment and comprises the following steps,
1) raw flue gas Q1Enters the first-stage heat exchanger 1 in the first heat exchanger group to exchange heat with the heat exchange medium in the first-stage heat exchanger 1, so that the original flue gas Q1Reducing the temperature to obtain low-temperature flue gas;
2) after the low-temperature flue gas is dedusted by the electric deduster 2, the low-temperature flue gas enters a rotary gas-gas heat exchanger 3 as a second heat exchanger group for heat exchange, so that the temperature of the flue gas is raised;
3) the heated flue gas is further heated by a compensation heating device 5 so as to reach a temperature range required by the denitration reaction, and the inlet flue gas temperature of the denitration reaction can better ensure the effect of the denitration reaction at 300-350 ℃;
4) the high-temperature flue gas flowing out of the denitration device 6 enters the rotary gas-gas heat exchanger 3 for heat exchange, the temperature of the flue gas is reduced, the flue gas with the reduced temperature enters the desulphurization device 7 for desulphurization reaction, and low-temperature clean flue gas Q is obtained2；
5)Low-temperature clean flue gas Q2The second-stage heat exchanger 8 entering the first heat exchanger group exchanges heat with a heat exchange medium, so that the low-temperature clean flue gas Q2The temperature rises and is discharged into the air.
As shown in fig. 2, in the raw flue gas Q1Before entering the first heat exchanger group, the original smoke Q is firstly determined1Temperature Tg, flow rate Q, SO3Concentration CSO3And pressure P, and determining the optimal reaction temperature range T according to the catalyst selected for denitration reactionmin～TmaxDetermining the acid dew point Ts according to an acid dew point prediction correlation, wherein the acid dew point prediction correlation is Ts ═ f (C)SO3P), judging the temperature Tg and the acid dew point Ts to obtain whether the initial operation state of the system is operated at a temperature above the acid dew point or below the acid dew point, and then, carrying out Q) on the original flue gas1Enters the first-stage heat exchanger 1 in the first heat exchanger group, does not need to adjust the heat exchange capacity of the first heat exchanger group at the moment, and directly carries out the adjustment on the original flue gas Q1Heat exchange and temperature reduction are carried out; then, the step 2) is carried out again, heat exchange is carried out through the rotary type gas-gas heat exchanger 3, and the temperature of the flue gas is raised to T3。
In step 3), it is necessary to treat T3Whether the reaction temperature is in the optimum reaction temperature range T of the denitration reactionmin～TmaxInternally judging, if not, heating by the compensating heating device 5 and correspondingly adjusting the compensating heating value to enable the T3Lifting until heated T is detected3At Tmin～TmaxWithin the temperature range of (3), the compensation heating value of the compensation heating device 5 is not required to be adjusted again, and the next step is carried out.
Further, in order to make the temperature judgment and adjustment more accurate, in step 3), a flue gas temperature threshold value at the inlet end of the compensation heating device 5 can be preset according to the temperature required at the inlet end of the denitration device 6, when the flue gas temperature at the inlet end of the compensation heating device 5 detected by the temperature sensor is lower than the flue gas temperature threshold value at the inlet end of the compensation heating device 5, the compensation heating device 5 is started, the compensation heating value of the compensation heating device 5 is adjusted according to the temperature difference, and the flue gas temperature value required at the inlet end of the denitration device 6 is ensured; when the compensation heating device 5 is a coal gas compensation heater, the flow of coal gas is adjusted through a valve, so that the flow of high-temperature gas after combustion is controlled, and the temperature of flue gas at the inlet of the denitration device 6 is ensured to be within a required temperature interval.
Further, on the basis of ensuring the flue gas temperature value required by the inlet end of the denitration device 6, the circulating flow rate of heat exchange media in the first-stage heat exchanger 1 and the second-stage heat exchanger 8 is adjusted through a water pump, so that the heat exchange capacity of the first heat exchanger group is adjusted, the flue gas temperature at the inlet end of the electric dust collector 2 is reduced, namely, the original flue gas temperature Tg is further reduced, the flue gas temperature at the inlet end of the electric dust collector 2 is below an acid dew point Ts, preferably below 120 ℃ in the embodiment, and therefore the dust removal efficiency of the electric dust collector 2 is further improved while high-efficiency denitration is ensured; when the flue gas temperature at the inlet end of the electric dust collector 2 is reduced, the temperature of the hot end of the first heat exchanger group is also increased, namely, the clean flue gas Q is increased2The smoke exhaust temperature further avoids the problem that smoke plume is generated due to the condensation of water vapor at the exhaust position of the smoke.
Further, when 6 entry end temperatures of denitrification facility and 2 entry end temperatures of electrostatic precipitator all guarantee in the best interval, can further adjust rotation type gas heat exchanger 3's heat transfer ability, improve the utilization ratio of flue gas self energy on the one hand, on the other hand can also guarantee that the mixed reaction of 4 alkaline powders of granule quenching and tempering device and flue gas is gone on in the best temperature interval, should locate the best operating temperature interval at 150 ~ 200 ℃.
The adaptability that carries out according to actual demand all is in the protection scope of the utility model.
The utility model discloses a concrete example is applied to explain the principle and the implementation mode of the utility model, and the explanation of the above example is only used to help understand the method and the core idea of the utility model; meanwhile, for the general technical personnel in the field, according to the idea of the present invention, there are changes in the concrete implementation and the application scope. In summary, the content of the present specification should not be construed as a limitation of the present invention.
Claims (7)
1. The utility model provides a sintering flue gas multi-pollutant ultralow discharge system which characterized in that: the electric dust collector comprises an electric dust collector, a compensation heating device, a denitration device and a desulfurization device which are sequentially arranged along the flowing direction of flue gas, wherein the inlet end of the electric dust collector is provided with a first heat exchanger group, and the high-temperature flue gas at the inlet end of the electric dust collector and the low-temperature flue gas at the outlet end of the desulfurization device exchange heat.
2. The system for ultralow emission of multiple pollutants in sintering flue gas as claimed in claim 1, wherein: the first heat exchanger group is in including setting up the one-level heat exchanger of electrostatic precipitator entry end and setting are in the second grade heat exchanger of desulphurization unit exit end, the one-level heat exchanger with the second grade heat exchanger intercommunication, just the one-level heat exchanger with heat transfer medium circulation heat transfer in the second grade heat exchanger.
3. The system for ultralow emission of pollutants in sintering flue gas as claimed in claim 1 or 2, wherein: and the inlet end of the compensation heating device and the outlet end of the denitration device are provided with a second heat exchanger group, and the second heat exchanger group exchanges heat between the low-temperature flue gas at the inlet end of the compensation heating device and the high-temperature flue gas at the outlet end of the denitration device.
4. The system for ultralow emission of multiple pollutants in sintering flue gas as claimed in claim 3, wherein: the second heat exchanger group is a rotary gas-gas heat exchanger.
5. The system for ultralow emission of multiple pollutants in sintering flue gas as claimed in claim 3, wherein: and a particle conditioning device for conditioning the flue gas is also arranged between the outlet end of the second heat exchanger group and the inlet end of the compensating heating device.
6. The system for ultralow emission of multiple pollutants in sintering flue gas as claimed in claim 5, wherein: the particle conditioning device comprises a Venturi tube, the inlet section of the Venturi tube is connected with the outlet end of the second heat exchanger group, the diffusion section of the Venturi tube is connected with the inlet end of the compensation heating device, and the throat part of the Venturi tube is connected with a container containing alkaline powder.
7. The system for ultralow emission of multiple pollutants in sintering flue gas as claimed in claim 6, wherein: the entry end of the electric dust collector, the entry end of the compensation heating device and the entry end of the denitration device are both provided with temperature sensors.
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