CN110575741A - Flue gas desulfurization and denitrification device and method - Google Patents
Flue gas desulfurization and denitrification device and method Download PDFInfo
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Abstract
The invention provides a flue gas desulfurization and denitration device and a flue gas desulfurization and denitration method, wherein the device comprises a desulfurization unit and a denitration unit, the desulfurization unit comprises a fluidized bed reactor, an adsorbent is filled in the fluidized bed reactor, and the bottom of the fluidized bed reactor is connected with a flue gas channel and an ozone channel; the denitration unit comprises a spraying device, and a flue gas outlet of the fluidized bed reactor is connected with a flue gas inlet of the spraying device. The invention leads the adsorbent to flow in a way of fluidized bed reactorThe flue gas to be treated is contacted with the chemical state, the mass transfer process is strengthened, and SO in the flue gas is absorbed2Meanwhile, ozone is added to oxidize low-valence nitrogen oxides NO, so that the subsequent spraying absorption of the nitrogen oxides is facilitated, and the desulfurization and denitrification efficiency of the flue gas is improved; the device has simple structure, is suitable for the treatment of flue gas at various temperatures, does not need to use a catalyst, and has lower cost.
Description
Technical Field
The invention belongs to the technical field of flue gas treatment, and relates to a flue gas desulfurization and denitrification device and a flue gas desulfurization and denitrification method.
Background
the industrial production of fossil fuel combustion, metal smelting and the like can generate a large amount of flue gas, wherein SO is contained in the flue gas2With NOxIs one of the main pollution sources of air pollution, can cause environmental problems such as haze, acid rain, photochemical smog and the like, seriously endangers the human health and the living environment, and therefore, the flue gas needs to be subjected to desulfurization and denitrification treatment before being discharged.
Aiming at the desulfurization and denitrification treatment of flue gas, the currently common desulfurization process comprises dry desulfurization, wet desulfurization, adsorption and the like, the denitrification process mainly comprises a selective catalytic reduction method, a selective non-catalytic reduction method and the like, the main sources of the flue gas comprise various industrial furnaces and coal-fired power plants, and due to the fact that the fluctuation range of the temperature and the concentration of the flue gas is large, the components are complex, catalyst poisoning is easily caused, the cost of the catalyst is high, the temperature of the flue gas is generally difficult to be within the active temperature range of the catalyst, the catalytic efficiency is limited, and additional treatment is needed before catalysis.
CN 107511064A discloses a desulfurization and denitrification method based on activated carbon and a low-temperature catalyst, which comprises the following steps: removing dust from the flue gas by gravity settling; mixing the flue gas with ammonia water and activated carbon, wherein the activated carbon is used as SO2Adsorbent of (2) and NOxReduction of the catalyst support with simultaneous removal of SO2、NOxAnd NH3Then separating the activated carbon to obtain purified flue gas, and the method uses the activated carbon as a carrier of the catalyst while desulfurizing, wherein the activated carbon is in a fluidized stateThe catalyst binding is weak and SO2The catalyst has obvious toxic action on the catalyst, so that the denitration effect of the catalyst is limited, and the waste of the catalyst can be caused.
CN 207856647U discloses a gaseous phase oxidation is absorption flue gas multi-pollutants purifier in coordination, include along flue gas direction set gradually flue gas air inlet, main air exhauster, flue gas passageway, absorption tower flue gas entry, flue gas outlet, be connected with the ozone oxidation system on the flue gas passageway, the ozone purification flue gas is jetted out to the flue gas passageway in to the ozone oxidation system, and the device adopts ozone oxidation flue gas component, and the reuse thick liquid absorbs, but the oxidation to components such as organic matter, heavy metal is difficult to go on under this reaction condition, and the flue gas is handled incompletely, even can partial oxidation also be with in concentrating into liquid with multiple harmful component, still do not separate, be difficult to direct utilization.
In summary, in the desulfurization and denitration treatment of flue gas, it is also necessary to perform treatment and recovery separately under the operation as simple as possible, so as to improve the efficiency of desulfurization and denitration.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a flue gas desulfurization and denitrification device and a flue gas desulfurization and denitrification method2Meanwhile, ozone is added to oxidize low-valence nitrogen oxides NO, so that the subsequent spraying absorption of the nitrogen oxides is facilitated, and the desulfurization and denitrification efficiency of the flue gas is improved; the device has simple structure, is suitable for the flue gas at various temperatures, and has lower cost.
In order to achieve the purpose, the invention adopts the following technical scheme:
on one hand, the invention provides a flue gas desulfurization and denitration device, which comprises a desulfurization unit and a denitration unit, wherein the desulfurization unit comprises a fluidized bed reactor, an adsorbent is filled in the fluidized bed reactor, and the bottom of the fluidized bed reactor is connected with a flue gas channel and an ozone channel; the denitration unit comprises a spraying device, and a flue gas outlet of the fluidized bed reactor is connected with a flue gas inlet of the spraying device.
In the invention, the main body of the device comprises a desulfurization unit and a denitration unit, and the adsorbent in the fluidized bed reactor is contacted with the flue gas to be treated in a fluidized state, thereby being beneficial to SO in the flue gas2The fluidized adsorbent can adsorb fine particles in the flue gas, and slightly larger particles are settled in the contact collision process with the adsorbent particles, so that the dust removal effect is achieved to a certain extent; simultaneously, the introduced ozone can oxidize NO in the flue gas, so that the NO is converted into absorbable high-valence nitrogen oxide, and the subsequent denitration process is completed.
The following technical solutions are preferred technical solutions of the present invention, but not limited to the technical solutions provided by the present invention, and technical objects and advantageous effects of the present invention can be better achieved and achieved by the following technical solutions.
as a preferable technical scheme of the invention, a gas distribution plate is arranged at the lower part of the fluidized bed reactor and is positioned above a gas inlet.
Preferably, the loading volume of the adsorbent in the fluidized bed reactor is 30-60%, for example, 30%, 35%, 40%, 45%, 50%, 55%, or 60%, but not limited to the recited values, and other values not recited in the range of values are also applicable.
in the present invention, the loading of the adsorbent is determined by factors such as the particle size, adsorption capacity, and fluidization degree of the adsorbent, and an appropriate loading is selected as needed.
Preferably, the adsorbent comprises activated coke and/or activated carbon.
In the present invention, SO is adsorbed by activated coke and/or activated carbon2after that, SO in the adsorbed state2Is easily oxidized into SO in the presence of ozone3the regenerated sulfuric acid is stored in the pores of the adsorbent and can be recovered during the regeneration of the adsorbent.
As a preferred technical solution of the present invention, the top of the spraying device is provided with at least one spraying head, for example, one, two, three or four spraying heads, and the number of the spraying heads is selected according to the cross section size of the spraying device, the size of a single spraying head, the amount of flue gas to be treated, the amount of added spraying liquid, and the like.
Preferably, the middle part of spray set is equipped with liquid distributor, plays the effect of redistributing to spraying liquid, helps flue gas denitration efficiency's improvement.
preferably, the bottom liquid outlet and the top liquid inlet of the spraying device are connected through a pipeline outside the spraying device.
in the invention, a pump is arranged on the circulating pipeline outside the spraying device to recycle the spraying liquid, and when the concentration of the spraying liquid is higher, new spraying liquid can be supplemented.
As a preferred technical scheme, the device also comprises an ozone generating device, and the ozone generating device is connected to the fluidized bed reactor through an ozone channel.
preferably, the outlet of the ozone channel is arranged on the flue gas channel.
in the invention, ozone is directly introduced into the oxygen pipeline, so that oxygen and ozone are mixed before entering the fluidized bed reactor, and the sufficient oxidation of NO is facilitated.
As the preferable technical scheme of the invention, the device also comprises a gas-solid separation device, wherein a flue gas outlet of the fluidized bed reactor is connected with the gas-solid separation device, and a gas outlet of the gas-solid separation device is connected with the spraying device.
Preferably, the gas-solid separation device comprises a cyclone.
In the invention, the adsorbent is in a fluidized state, and part of particles easily leave the fluidized bed reactor along with the desulfurized flue gas, so that a gas-solid separation device is arranged behind the fluidized bed reactor to settle the adsorbent particles and the dust in the flue gas, thereby avoiding the waste of the adsorbent entering a spraying device and further removing the residual dust.
As a preferable technical scheme, the device also comprises an adsorbent regeneration device, an adsorbent outlet of the fluidized bed reactor is connected with an inlet of the adsorbent regeneration device, and an outlet of the adsorbent regeneration device is connected with an adsorbent inlet of the fluidized bed reactor.
In the invention, the adsorbent activated carbon and/or activated coke can enter the adsorbent regeneration device for regeneration after being adsorbed and saturated, the sulfuric acid in the pores of the adsorbent can be recovered during regeneration, and the regenerated adsorbent can be recycled.
In another aspect, the present invention provides a method for desulfurization and denitrification by using the above apparatus, the method comprising the following steps:
(1) After the flue gas to be treated and the ozone enter the fluidized bed reactor, the adsorbent is in a fluidized state and adsorbs SO in the process of contacting with the flue gas2Ozone oxidation of NOxobtaining desulfurized flue gas;
(2) And (3) absorbing the desulfurized flue gas obtained in the step (1) by adopting a spraying liquid to obtain purified gas.
as a preferable technical scheme of the invention, SO in the flue gas to be treated in the step (1)2the concentration of (A) is 500-2000 mg/Nm3E.g. 500mg/Nm3、750mg/Nm3、1000mg/Nm3、1200mg/Nm3、1500mg/Nm3、1800mg/Nm3Or 2000mg/Nm3and the like, but are not limited to the recited values, and other unrecited values within the numerical range are equally applicable; NOxThe concentration of (A) is 200-350 mg/Nm3E.g. 200mg/Nm3、220mg/Nm3、250mg/Nm3、280mg/Nm3、300mg/Nm3、320mg/Nm3Or 350mg/Nm3And the like, but are not limited to the recited values, and other values not recited within the numerical range are also applicable.
Preferably, the temperature of the flue gas to be treated in the step (1) is 80-200 ℃, for example, 80 ℃, 100 ℃, 120 ℃, 140 ℃, 160 ℃, 180 ℃ or 200 ℃, but is not limited to the recited values, and other values not recited in the range of the values are also applicable.
In the invention, because the denitration by using a catalyst is not used, the temperature of the flue gas is not strictly limited, the flue gas generated by a common coal-fired power plant or an industrial kiln can be treated, and the heat exchange treatment is not required to be carried out in advance.
Preferably, the ozone is introduced into the flue gas in the step (1) in an amount corresponding to the NO in the flue gasxThe molar ratio of (1 to 2):1, for example, 1:1, 1.2:1, 1.4:1, 1.6:1, 1.8:1 or 2:1, but is not limited to the numerical values listed, and other numerical values not listed in the numerical value range are also applicable.
Preferably, the desulfurized flue gas obtained in the step (1) is subjected to gas-solid separation, the obtained gas phase is subjected to denitration, and the obtained solid phase returns to the fluidized bed reactor.
As a preferable technical scheme of the invention, the adsorbent in the step (1) comprises activated coke and/or activated carbon.
Preferably, the adsorbent is saturated and discharged for regeneration.
Preferably, the temperature at which the adsorbent is regenerated is 300 to 450 ℃, such as 300 ℃, 320 ℃, 350 ℃, 380 ℃, 400 ℃, 425 ℃ or 450 ℃, but not limited to the recited values, and other values not recited within the range of values are equally applicable; the regeneration time is 0.5 to 2 hours, for example, 0.5 hour, 0.8 hour, 1 hour, 1.5 hour, 1.8 hour or 2 hours, but is not limited to the values listed, and other values not listed in the numerical range are also applicable.
As a preferable technical scheme of the invention, the spraying liquid in the step (2) comprises an alkali solution and/or an alkali metal carbonate solution.
Preferably, the spray liquid in the step (2) comprises Ca (OH)2Solution, NaOH solution, Na2CO3any one of solutions or aqueous ammonia or a combination of at least two of these, typical but non-limiting examples being: ca (OH)2combination of solution and NaOH solution, NaOH solution and Na2CO3Combination of solutions, Ca (OH)2solution, combination of NaOH solution and ammonia water, NaOH solution, Na2CO3combinations of solutions and ammonia, and the like.
In the invention, the nitrogen oxides in the smoke after ozone oxidation comprise NO2、N2O3、N2O5and the nitrate or nitrite can be absorbed by the alkali liquor to generate nitrate or nitrite, and the removal mode is simpler.
Preferably, the mass concentration of the spray liquid in the step (2) is 3 to 10 wt%, such as 3 wt%, 4 wt%, 5 wt%, 6 wt%, 8 wt% or 10 wt%, but not limited to the recited values, and other values not recited in the range of the recited values are also applicable.
Preferably, the temperature at which the absorption in step (2) is carried out by using the spray liquid is 20 to 80 ℃, for example, 20 ℃, 30 ℃, 40 ℃, 50 ℃, 60 ℃, 70 ℃ or 80 ℃, but is not limited to the recited values, and other values not recited in the range of the values are also applicable.
Compared with the prior art, the invention has the following beneficial effects:
(1) The invention leads the adsorbent to be contacted with the flue gas to be treated in a fluidized state through the arrangement of the fluidized bed reactor, strengthens the mass transfer process and adsorbs SO in the flue gas2Meanwhile, ozone is added to oxidize low-valence nitrogen oxides NO, so that the subsequent spraying absorption of the nitrogen oxides is facilitated, the desulfurization and denitrification efficiency of the flue gas is improved, the desulfurization efficiency can reach more than 98%, and the denitrification efficiency can reach more than 91%;
(2) The device has simple structure, is suitable for treating the flue gas at various temperatures, does not need to use a catalyst, and has lower cost.
Drawings
FIG. 1 is a schematic structural diagram of a flue gas desulfurization and denitrification apparatus provided in embodiment 1 of the present invention;
The system comprises a fluidized bed reactor 1, an ozone generating device 2, a gas-solid separating device 3, a spraying device 4 and an adsorbent regenerating device 5.
Detailed Description
In order to better illustrate the present invention and facilitate the understanding of the technical solution of the present invention, the following embodiments further describe the present invention in detail, but the following examples are only simple examples of the present invention and do not represent or limit the scope of the present invention, and the scope of the present invention is subject to the claims.
The invention provides a flue gas desulfurization and denitration device and a flue gas desulfurization and denitration method, wherein the device comprises a desulfurization unit and a denitration unit, the desulfurization unit comprises a fluidized bed reactor 1, an adsorbent is filled in the fluidized bed reactor 1, and the bottom of the fluidized bed reactor 1 is connected with a flue gas channel and an ozone channel; the denitration unit comprises a spraying device 4, and a flue gas outlet of the fluidized bed reactor 1 is connected with a flue gas inlet of the spraying device 4.
The method comprises the following steps:
(1) After the flue gas to be treated and the ozone enter the fluidized bed reactor 1, the adsorbent is in a fluidized state and adsorbs SO in the process of contacting with the flue gas2ozone oxidation of NOxObtaining desulfurized flue gas;
(2) And (3) absorbing the desulfurized flue gas obtained in the step (1) by adopting a spraying liquid to obtain purified gas.
The following are typical but non-limiting examples of the invention:
Example 1:
The embodiment provides a flue gas desulfurization and denitration device, the structural schematic diagram of the device is shown in fig. 1, and the device comprises a desulfurization unit and a denitration unit, wherein the desulfurization unit comprises a fluidized bed reactor 1, an adsorbent is filled in the fluidized bed reactor 1, and the bottom of the fluidized bed reactor 1 is connected with a flue gas channel and an ozone channel; the denitration unit comprises a spraying device 4, and a flue gas outlet of the fluidized bed reactor 1 is connected with a flue gas inlet of the spraying device 4.
A gas distribution plate is arranged at the lower part of the fluidized bed reactor 1 and is positioned above a gas inlet; the filling volume of the adsorbent in the fluidized bed reactor 1 accounts for 50%, and the adsorbent is activated coke.
The top of the spraying device 4 is provided with three spraying heads which are arranged in a triangular shape; the middle part of the spraying device 4 is provided with a liquid distributor; and a liquid outlet at the bottom of the spraying device 4 is connected with a liquid inlet at the top of the spraying device 4 through a pipeline, and a pump is arranged on the pipeline.
The device also comprises an ozone generating device 2, and the ozone generating device 2 is connected to the smoke channel through an ozone channel.
The device also comprises a gas-solid separation device 3, wherein a flue gas outlet of the fluidized bed reactor 1 is connected with the gas-solid separation device 3, and a gas outlet of the gas-solid separation device 3 is connected with a spraying device 4; the gas-solid separation device 3 is a cyclone separator.
The device also comprises an adsorbent regeneration device 5, wherein an adsorbent outlet of the fluidized bed reactor 1 is connected with an inlet of the adsorbent regeneration device 5, and an outlet of the adsorbent regeneration device 5 is connected with an adsorbent inlet of the fluidized bed reactor 1.
Example 2:
The embodiment provides a flue gas desulfurization and denitration device, which comprises a desulfurization unit and a denitration unit, wherein the desulfurization unit comprises a fluidized bed reactor 1, an adsorbent is filled in the fluidized bed reactor 1, and the bottom of the fluidized bed reactor 1 is connected with a flue gas channel and an ozone channel; the denitration unit comprises a spraying device 4, and a flue gas outlet of the fluidized bed reactor 1 is connected with a flue gas inlet of the spraying device 4.
A gas distribution plate is arranged at the lower part of the fluidized bed reactor 1 and is positioned above a gas inlet; the filling volume of the adsorbent in the fluidized bed reactor 1 accounts for 30%, and the adsorbent is activated carbon.
The top of the spraying device 4 is provided with five spraying heads which are uniformly distributed in the same cross section; the middle part of the spraying device 4 is provided with a liquid distributor; and a liquid outlet at the bottom of the spraying device 4 is connected with a liquid inlet at the top of the spraying device 4 through a pipeline, and a pump is arranged on the pipeline.
The apparatus further comprises an ozone generating device 2, said ozone generating device 2 being connected to the lower ozone inlet of the fluidized bed reactor 1 via an ozone channel.
The device also comprises a gas-solid separation device 3, wherein a flue gas outlet of the fluidized bed reactor 1 is connected with the gas-solid separation device 3, and a gas outlet of the gas-solid separation device 3 is connected with a spraying device 4; the gas-solid separation device 3 is a cyclone separator.
The device also comprises an adsorbent regeneration device 5, wherein an adsorbent outlet of the fluidized bed reactor 1 is connected with an inlet of the adsorbent regeneration device 5, and an outlet of the adsorbent regeneration device 5 is connected with an adsorbent inlet of the fluidized bed reactor 1.
Example 3:
the embodiment provides a flue gas desulfurization and denitration method, wherein the flue gas is sintering flue gas, and the flow rate of the flue gas is 20000Nm3The method is carried out by using the device in the embodiment 1 and comprises the following steps:
(1) after the flue gas to be treated and the ozone enter the fluidized bed reactor 1, SO in the flue gas2At a concentration of 1000mg/Nm3，NOxAt a concentration of 300mg/Nm3The temperature of the flue gas is 150 ℃, and NO in the ozone flue gas is introduced into the flue gas at the same timexThe molar ratio of the active coke to the flue gas is 1.5:1, the active coke of the adsorbent is in a fluidized state and adsorbs SO in the contact process of the active coke and the flue gas2Ozone oxidation of NOxObtaining desulfurized flue gas;
(2) And (3) discharging the activated coke saturated in the step (1) into an adsorbent regeneration device 5 for regeneration, wherein the regeneration temperature is 400 ℃, the regeneration time is 1h, and the obtained regenerated activated coke returns to the step (1).
(3) Cyclone separation is carried out on the desulfurized flue gas obtained in the step (1), active coke and dust carried in the flue gas are separated, and then 5 wt% of Ca (OH) is adopted2Solution as spray liquid for absorbing NOxand the absorption temperature is 50 ℃, so that the desulfurization and denitrification purified gas is obtained.
In this embodiment, after the flue gas is subjected to desulfurization and denitrification, the flue gas is treated according to SO in the purified gas2And NOxIs calculated to obtain SO2The removal rate of the catalyst reaches 98.5 percent, and NO isxThe removal rate of the catalyst reaches 91.8 percent, and the final dust content is lower than 15mg/Nm3。
example 4:
The embodiment provides a flue gas desulfurization and denitration method, the used flue gas is flue gas of a coal-fired power plant, and the flow rate of the flue gas is 25000Nm3The method is carried out by adopting the device in the embodiment 2 and comprises the following steps:
(1) after the flue gas to be treated and the ozone enter the fluidized bed reactor 1, SO in the flue gas2At a concentration of 500mg/Nm3，NOxAt a concentration of 200mg/Nm3The temperature of the flue gas is 100 ℃, and NO in the ozone flue gas is introduced into the flue gas at the same timexThe molar ratio of the active coke to the flue gas is 1.2:1, the active coke of the adsorbent is in a fluidized state and adsorbs SO in the contact process of the active coke and the flue gas2Ozone oxidation of NOxObtaining desulfurized flue gas;
(2) And (3) discharging the saturated activated carbon adsorbed in the step (1) into an adsorbent regenerating device 5 for regeneration, wherein the regeneration temperature is 300 ℃, the regeneration time is 2 hours, and the obtained regenerated activated carbon returns to the step (1).
(3) Performing cyclone separation on the desulfurized flue gas obtained in the step (1), separating active coke and dust carried in the flue gas, and then adopting NaOH solution and Na with the concentration of 3 wt% and the volume ratio of 1:12CO3solution as spray liquid for absorbing NOxAnd the absorption temperature is 30 ℃, so that the desulfurization and denitrification purified gas is obtained.
In this embodiment, after the flue gas is subjected to desulfurization and denitrification, the flue gas is treated according to SO in the purified gas2And NOxIs calculated to obtain SO2The removal rate of the catalyst reaches 98.8 percent, and NO is reducedxThe removal rate of the catalyst reaches 92.3 percent, and the final dust content is lower than 10mg/Nm3。
Example 5:
The embodiment provides a flue gas desulfurization and denitration method, wherein the flue gas is kiln flue gas, and the flue gas flow is 15000Nm3The method is carried out by using the device in the embodiment 1 and comprises the following steps:
(1) After the flue gas to be treated and the ozone enter the fluidized bed reactor 1, SO in the flue gas2At a concentration of 2000mg/Nm3，NOxAt a concentration of 350mg/Nm3the temperature of the flue gas is 200 ℃, and NO in the ozone flue gas is introduced into the flue gas at the same timexThe molar ratio of the active coke to the flue gas is 2:1, the active coke of the adsorbent is in a fluidized state and adsorbs SO in the contact process of the active coke and the flue gas2Ozone oxidation of NOxObtaining desulfurized flue gas;
(2) and (3) discharging the activated coke subjected to adsorption saturation in the step (1) into an adsorbent regeneration device 5 for regeneration, wherein the regeneration temperature is 450 ℃, the regeneration time is 0.5h, and the obtained regenerated activated coke is returned to the step (1).
(3) Performing cyclone separation on the desulfurized flue gas obtained in the step (1) to separate active coke and dust carried in the flue gasthen, ammonia water solution with the concentration of 10 wt% is used as spraying liquid to absorb NOxAnd the absorption temperature is 80 ℃, so that the purified gas for desulfurization and denitrification is obtained.
In this embodiment, after the flue gas is subjected to desulfurization and denitrification, the flue gas is treated according to SO in the purified gas2And NOxIs calculated to obtain SO2The removal rate of the catalyst reaches 98.1 percent, and NOxthe removal rate of the catalyst reaches 91.4 percent, and the final dust content is lower than 13mg/Nm3。
Comparative example 1:
This comparative example provides a flue gas desulfurization and denitrification apparatus and method, the structure of the apparatus is as in example 1, except that: the desulfurization unit includes a fixed bed reactor.
The process is referred to the process in example 3, with the only difference that: the desulfurization and oxidation processes in the step (1) are carried out in a fixed bed reactor.
In the comparative example, the contact and reaction degree of the adsorbent and oxygen are weakened due to different reactor types and material motion states in the reaction process, so that the flue gas desulfurization efficiency and NO are reducedxthe oxidation rate of (2) is reduced, and at the moment, the desulfurization efficiency of the flue gas is only 84.5%, and the denitration efficiency is only 77.2%.
It can be seen from the above examples and comparative examples that the invention makes the adsorbent contact with the flue gas to be treated in a fluidized state by the arrangement of the fluidized bed reactor, thereby strengthening the mass transfer process and adsorbing SO in the flue gas2Meanwhile, ozone is added to oxidize low-valence nitrogen oxides NO, so that the subsequent spraying absorption of the nitrogen oxides is facilitated, the desulfurization and denitrification efficiency of the flue gas is improved, the desulfurization efficiency can reach more than 98%, and the denitrification efficiency can reach more than 91%; the device has simple structure, is suitable for the treatment of flue gas at various temperatures, does not need to use a catalyst, and has lower cost.
The applicant states that the present invention is described in detail by the above embodiments, but the present invention is not limited to the above detailed apparatus and method, i.e. it is not meant to imply that the present invention must be implemented by the above detailed apparatus and method. It will be understood by those skilled in the art that any modifications to the present invention, equivalent alterations to the device of the present invention, additions of auxiliary components, selection of particular modes, etc., are within the scope and disclosure of the present invention.
Claims (10)
1. A flue gas desulfurization and denitrification device is characterized by comprising a desulfurization unit and a denitrification unit, wherein the desulfurization unit comprises a fluidized bed reactor, an adsorbent is filled in the fluidized bed reactor, and the bottom of the fluidized bed reactor is connected with a flue gas channel and an ozone channel; the denitration unit comprises a spraying device, and a flue gas outlet of the fluidized bed reactor is connected with a flue gas inlet of the spraying device.
2. The apparatus of claim 1, wherein a gas distribution plate is provided at a lower portion of the fluidized bed reactor, the gas distribution plate being located above the gas inlet;
Preferably, the filling volume of the adsorbent in the fluidized bed reactor accounts for 30-60%;
Preferably, the adsorbent comprises activated coke and/or activated carbon.
3. The device of claim 1 or 2, wherein the top of the spraying device is provided with at least one spraying head;
Preferably, a liquid distributor is arranged in the middle of the spraying device;
Preferably, the bottom liquid outlet and the top liquid inlet of the spraying device are connected through a pipeline outside the spraying device.
4. the apparatus according to any one of claims 1 to 3, further comprising an ozone generating device connected to the fluidized bed reactor through an ozone channel;
Preferably, the outlet of the ozone channel is arranged on the flue gas channel.
5. The device according to any one of claims 1 to 4, further comprising a gas-solid separation device, wherein the flue gas outlet of the fluidized bed reactor is connected with the gas-solid separation device, and the gas outlet of the gas-solid separation device is connected with the spraying device;
Preferably, the gas-solid separation device comprises a cyclone.
6. The apparatus of any one of claims 1 to 5, further comprising an adsorbent regeneration unit, wherein the adsorbent outlet of the fluidized bed reactor is connected to the inlet of the adsorbent regeneration unit, and wherein the outlet of the adsorbent regeneration unit is further connected to the adsorbent inlet of the fluidized bed reactor.
7. A method for desulfurization and denitrification by using the apparatus according to any one of claims 1 to 6, characterized by comprising the steps of:
(1) After the flue gas to be treated and the ozone enter the fluidized bed reactor, the adsorbent is in a fluidized state and adsorbs SO in the process of contacting with the flue gas2Ozone oxidation of NOxObtaining desulfurized flue gas;
(2) And (3) absorbing the desulfurized flue gas obtained in the step (1) by adopting a spraying liquid to obtain purified gas.
8. The method according to claim 7, wherein SO in the flue gas to be treated in the step (1)2the concentration of (A) is 500-2000 mg/Nm3，NOxThe concentration of (A) is 200-350 mg/Nm3；
Preferably, the temperature of the flue gas to be treated in the step (1) is 80-200 ℃;
Preferably, the ozone is introduced into the flue gas in the step (1) in an amount corresponding to the NO in the flue gasxThe molar ratio of (1-2) to (1);
Preferably, the desulfurized flue gas obtained in the step (1) is subjected to gas-solid separation, the obtained gas phase is subjected to denitration, and the obtained solid phase returns to the fluidized bed reactor.
9. The process of claim 7 or 8, wherein the adsorbent of step (1) comprises activated coke and/or activated carbon;
Preferably, the adsorbent is discharged for regeneration after being saturated in adsorption;
preferably, the regeneration temperature of the adsorbent is 300-450 ℃, and the regeneration time is 0.5-2 h.
10. The method according to any one of claims 7 to 9, wherein the spray liquid of step (2) comprises an alkali solution and/or a carbonate solution of an alkali metal;
Preferably, the spray liquid in the step (2) comprises Ca (OH)2Solution, NaOH solution, Na2CO3Solution or ammonia water or the combination of at least two of the solutions and the ammonia water;
preferably, the mass concentration of the spraying liquid in the step (2) is 3-10 wt%;
Preferably, the temperature for absorbing by adopting the spray liquid in the step (2) is 20-80 ℃.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111495135A (en) * | 2020-04-23 | 2020-08-07 | 山东大学 | Three-phase flow NH3With NO, SO3Cooperative purification system and method and application |
| CN114130173A (en) * | 2021-12-08 | 2022-03-04 | 厦门理工学院 | Hydrogen sulfide gas absorption method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105126560A (en) * | 2015-07-24 | 2015-12-09 | 山东大学 | Ozone multipoint-adding sectional-oxidizing NOx absorption and removal system and ozone-multipoint-adding sectional-oxidizing NOx absorption and removal method |
| WO2016011681A1 (en) * | 2014-07-21 | 2016-01-28 | 中国科学院过程工程研究所 | Equipment and method for circulating fluidized bed semidry simultaneous desulfurization and denitration of sintering flue gas |
| CN108722114A (en) * | 2018-08-08 | 2018-11-02 | 国家能源投资集团有限责任公司 | Powdered activated coke adsorpting desulfurization device and the method that absorption desulfurization is carried out to flue gas using it |
| CN109529575A (en) * | 2018-12-26 | 2019-03-29 | 宁波大学 | Civil boiler for warming system for desulfuration and denitration |
-
2019
- 2019-09-29 CN CN201910936776.7A patent/CN110575741A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016011681A1 (en) * | 2014-07-21 | 2016-01-28 | 中国科学院过程工程研究所 | Equipment and method for circulating fluidized bed semidry simultaneous desulfurization and denitration of sintering flue gas |
| CN105126560A (en) * | 2015-07-24 | 2015-12-09 | 山东大学 | Ozone multipoint-adding sectional-oxidizing NOx absorption and removal system and ozone-multipoint-adding sectional-oxidizing NOx absorption and removal method |
| CN108722114A (en) * | 2018-08-08 | 2018-11-02 | 国家能源投资集团有限责任公司 | Powdered activated coke adsorpting desulfurization device and the method that absorption desulfurization is carried out to flue gas using it |
| CN109529575A (en) * | 2018-12-26 | 2019-03-29 | 宁波大学 | Civil boiler for warming system for desulfuration and denitration |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111495135A (en) * | 2020-04-23 | 2020-08-07 | 山东大学 | Three-phase flow NH3With NO, SO3Cooperative purification system and method and application |
| CN111495135B (en) * | 2020-04-23 | 2021-09-28 | 山东大学 | Three-phase flow NH3With NO, SO3Cooperative purification system and method and application |
| CN114130173A (en) * | 2021-12-08 | 2022-03-04 | 厦门理工学院 | Hydrogen sulfide gas absorption method |
| CN114130173B (en) * | 2021-12-08 | 2023-05-16 | 厦门理工学院 | Hydrogen sulfide gas absorption method |
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