CN211837168U - Active material generating device containing plasma generating equipment and flue gas denitration device - Google Patents
Active material generating device containing plasma generating equipment and flue gas denitration device Download PDFInfo
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- CN211837168U CN211837168U CN202020234100.1U CN202020234100U CN211837168U CN 211837168 U CN211837168 U CN 211837168U CN 202020234100 U CN202020234100 U CN 202020234100U CN 211837168 U CN211837168 U CN 211837168U
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Abstract
The utility model discloses an active material who contains plasma generating equipment produces device and flue gas denitration device. The utility model discloses an active material produces device includes: an oxidant generation device and a plasma excitation device. The utility model discloses a flue gas denitration device produces device, oxidation equipment, nitrogen oxide absorption equipment and dust removal and discharging equipment including the active material who contains plasma generating equipment. The utility model discloses an active material produces device and flue gas denitration device's operational safety is high.
Description
Technical Field
The utility model relates to an active material produces device and flue gas denitration device, especially an active material who contains plasma generating apparatus produces device and flue gas denitration device.
Background
Nitrogen oxides (NOx) can have adverse effects on the atmospheric environment and can be harmful to human health. The nitrogen oxides are mainly from flue gas discharged by coal-fired boilers, industrial kilns and steel sintering and pelletizing equipment.
Currently, the mainstream denitration technology is selective catalytic reduction denitration technology (SCR) or selective non-catalytic reduction denitration technology (SNCR). The SCR method has high denitration efficiency and small secondary pollution, but has high equipment investment cost and needs to use a catalyst. Due to the loss of activity of the catalyst, replacement is required due to expiration, and the operation and maintenance cost is high. The SNCR method has less investment and operation cost, but has lower denitration efficiency. The removal efficiency of the two denitration technologies can reach the emission standard established by the state at present, but the technology is complex, the control condition is harsh, the operation cost is high, the occupied area is large, and the denitration technology is not suitable for reconstruction projects. Under the condition of continuously improving the emission standard, research and development of a denitration device and a denitration process which are high in efficiency, good in economical efficiency and good in safety become key work of the environmental protection industry.
CN102327735A discloses a flue gas desulfurization and denitration system based on hydrogen peroxide effect. The system comprises a flue gas generation device, a dust remover connected with the flue gas generation device through a flue, an absorption tower connected with the dust remover through the flue, wherein the top of the absorption tower is connected with a chimney, the bottom of the absorption tower is connected with an oxidation fan and a liquid dust removal device, the liquid dust removal device is connected with a salt solution concentration crystallization device, the salt solution concentration crystallization device is connected with a finished product packaging device, the flue is connected with a hydrogen peroxide storage tank, and the hydrogen peroxide storage tank is used for providing a hydrogen peroxide solution and enabling the hydrogen peroxide solution to be vaporized to form hydrogen peroxide gas after entering the flue. This system uses hydrogen peroxide, which is unstable and decomposes to H above 120 ℃2O and O2Loss of NO oxidizedXThe ability of the cell to perform. The dust can cause H2O2Itself and hydroxyl radicals OH and O2H instantAggregation is inactivated. The temperature of the flue gas in the flue is just in the temperature range, the dust content is higher, and the H is greatly reduced2O2The oxidation performance of (2) is poor in economical efficiency.
CN109745840A discloses a treatment device for blast furnace gas incineration flue gas. Comprises a plasma reaction device, a gas inlet and a gas outlet, wherein the gas inlet is used for receiving flue gas generated by burning blast furnace gas; the absorption tower is provided with an inlet at the lower end, an ash discharge port and an outlet at the upper end, the outlet of the plasma reaction device is communicated with the inlet of the absorption tower through a flue, the lower part of the absorption tower is provided with a dry powder feeding port, a circulating fly ash feed back port and an atomization humidification inlet, the atomization humidification inlet is connected with an atomization humidification system, the atomization humidification system is used for spraying water into the absorption tower, the dry powder feeding port is connected with the dry powder feeding system, the dry powder feeding system is used for spraying alkaline dry powder into the absorption tower, and the absorption tower is used for trapping acidic substances and residual SO in the flue gas treated by the low-temperature plasma reaction device2And introducing the flue gas treated by the absorption tower into a cloth bag dust removal device, and discharging the flue gas after dust removal. In the patent document, flue gas is directly introduced into a low-temperature plasma reaction device for desulfurization and denitrification, the denitrification efficiency is only about 50%, and the production safety is poor.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects of the prior art, the utility model discloses an active material generating device who contains plasma generating equipment is provided to an object of this utility model. Another object of the utility model is to provide a flue gas denitration device. The utility model discloses an active material produces device and flue gas denitration device operational safety is high. Furthermore, the utility model discloses a flue gas denitration device's denitration efficiency is higher, and is suitable for NOx concentration more than or equal to 100mg/Nm3The flue gas denitration.
The utility model provides an active substance produces device, include:
an oxidant generation apparatus including an air supply unit and a reaction unit; the reaction unit is used for generating an oxidant; the air supply unit is used for supplying compressed air to the reaction liquid in the reaction unit to promote the generation of the oxidant and supplying air for adjusting to the vicinity of a mixed gas outlet of the reaction unit so as to adjust the concentration of the oxidant in a mixture formed by the air and the oxidant and form mixed gas containing the oxidant;
a plasma excitation apparatus includes a plasma generator for exciting a mixed gas containing an oxidant to form a gas containing an active substance.
According to the active material generating apparatus of the present invention, preferably, the reaction unit is provided with a compressed air inlet and a conditioning air inlet; the air supply unit includes an air compressor and a blower; the air compressor is connected with the compressed air inlet and is used for blowing compressed air into the reaction liquid of the reaction unit so as to promote the generation of an oxidant; the blower is connected with the regulating air inlet and used for supplying regulating air to the vicinity of the mixed gas outlet of the reaction unit so as to regulate the concentration of the oxidant in the mixture formed by the air and the oxidant and form mixed gas containing the oxidant.
According to the active material generating apparatus of the present invention, preferably, the reaction unit is a horizontal advection multistage reactor, at least one partition is provided in the reaction unit, and the partition is used for dividing the internal space of the reaction unit into a plurality of compartments; in these compartments, at least a part of the compartments are provided with a catalyst for catalyzing the reaction feed to obtain an oxidant; wherein the catalyst is a honeycomb catalyst.
According to the utility model discloses an active material produces device, preferably, be provided with the baffling pipe between the compartment, the baffling pipe is used for overflowing the reaction feed liquid of previous compartment to next compartment.
According to the active material generating apparatus of the present invention, preferably, the reaction unit is further provided with a steam inlet configured to be able to supply steam for heating to the reaction unit; the oxidant generating equipment also comprises a draught fan which is connected with the mixed gas outlet and used for conveying the mixed gas containing the oxidant to the plasma excitation equipment.
According to the active material generating apparatus of the present invention, preferably, the oxidant generating device further includes a mother liquor circulating device including a mother liquor tank and a mother liquor pump; the mother liquor tank is provided with a mother liquor inlet and a mother liquor outlet; the mother liquor outlet is connected with the mother liquor pump; the reaction unit is provided with a feed liquid outlet; the feed liquid outlet is connected with the mother liquid inlet, so that at least one part of reaction feed liquid is led out to a mother liquid tank; the reaction unit is also provided with a feed liquid inlet; and the feed liquid inlet is connected with the mother liquid pump and used for circulating the mother liquid in the mother liquid tank to the reaction unit.
According to the active material generating apparatus of the present invention, preferably, the oxidizing agent generating device further includes a first material supplying device containing a material a, a second material supplying device containing a material C, a third material supplying device containing a material B, and a fourth material supplying device containing a material S; a plurality of feed inlets are formed in the side wall of the reaction unit; the first material supply device, the second material supply device, the third material supply device and the fourth material supply device are respectively arranged to be capable of being connected with the feed ports so as to supply the material A, the material C, the material B and the material S to the reaction unit.
The utility model also provides a flue gas denitration device, it includes:
an active material generating device as described above; and
the oxidation device is connected with the plasma generator and is arranged to mix the gas containing the active substances and the flue gas to be treated so as to form oxidized flue gas; and
and the nitrogen oxide absorption equipment is connected with the oxidation equipment and is set to be capable of carrying out denitration treatment on the oxidized flue gas so as to form denitrated flue gas.
According to the utility model discloses a flue gas denitration device, preferably, nitrogen oxide absorption equipment includes absorption tower, absorbent storehouse and water supply equipment; the absorption tower is a circulating fluidized bed absorption tower; the absorption tower is provided with a flue gas inlet and a flue gas outlet; the oxidation equipment is connected with the flue gas inlet and is arranged to convey the oxidized flue gas to the absorption tower; the absorbent bin is connected with the absorption tower and is arranged to supply powdery absorbent to the absorption tower; the water supply device is arranged to spray water into the absorption tower so as to humidify the absorbent and the oxidized flue gas.
According to the utility model discloses a flue gas denitration device, preferably, still including dust removal and discharging equipment, it links to each other with nitrogen oxide absorption equipment, handles the flue gas after the denitration for purifying flue gas and discharging it.
The utility model discloses avoid directly letting in plasma generator with the flue gas, the oxidant concentration in the control mist avoids the danger that arouses because of oxidant concentration such as chlorine dioxide is too high, therefore the utility model discloses an active material produces device and flue gas denitration device's operational safety is high. Furthermore, the utility model discloses a denitration efficiency is higher, and is suitable for nitrogen oxide (NOx) concentration more than or equal to 100mg/Nm3The flue gas denitration.
Drawings
Fig. 1 is a schematic structural diagram of an active material generating apparatus including a plasma generating device according to the present invention.
Fig. 2 is the utility model discloses a flue gas denitration device's schematic structure diagram.
The reference numerals are explained below:
100-oxidant generation device, 200-plasma excitation device, 300-oxidation device, 400-nitrogen oxide absorption device, 500-dedusting and discharge device, 1-first material supply device, 2-second material supply device, 3-third material supply device, 4-fourth material supply device, 5-catalyst fixing position, 6-first supply pump, 7-second supply pump, 8-third supply pump, 9-fourth supply pump, 10-reaction unit, 11-steam inlet, 12-blower, 13-air compressor, 14-mother liquor tank, 15-mother liquor pump, 16-draught fan, 17-plasma generator, 18-oxidation device, 19-absorbent bin, 20-water supply device, 21-absorption tower, 22-bag dust collector, 23-byproduct bin and 24-chimney.
Detailed Description
The invention will be further described with reference to the drawings and the following examples, but the scope of the invention is not limited thereto.
The device is a product, namely a set of devices. The utility model provides a "vol%" is volume percentage content. In the present invention, the nitrogen oxide in a lower valence state means nitrogen oxide in a lower valence state (including trivalent), including nitrogen oxides in a lower valence state (NO) such as NOX) (ii) a The higher nitrogen oxide means nitrogen oxide with nitrogen being more than four (containing four valence) and including NO2、N2O5Nitrogen Oxides (NO) of equal valence stateX)。
Active material generating device
The active material generating device of the utility model comprises an oxidant generating device and a plasma exciting device. As described in detail below.
Oxidant generating equipment
The utility model discloses an oxidant generating equipment includes reaction unit and air supply unit. The reaction unit is used for generating an oxidizing agent. The air supply unit is used for supplying air to the reaction unit. Specifically, the air supply unit supplies compressed air to the reaction feed liquid in the reaction unit to promote the generation of the oxidant, and supplies conditioning air to the vicinity of the mixed gas outlet of the reaction unit to adjust the concentration of the oxidant in the mixture of air and the oxidant, forming the mixed gas containing the oxidant.
The reaction unit of the utility model is provided with a compressed air inlet and an air inlet for adjustment. The air supply unit comprises an air compressor and a blower, wherein the air compressor is connected with a compressed air inlet and is used for blowing compressed air into the reaction liquid of the reaction unit so as to promote the generation of the oxidant. The blower is connected with the regulating air inlet and is used for supplying regulating air to the vicinity of the mixed gas outlet of the reaction unit so as to regulate the oxidant concentration in the mixture formed by the air and the oxidant and form mixed gas containing the oxidant.
In certain embodiments, the reaction unit is provided with a compressed air inlet at an upper portion of the sidewall. An air compressor is connected to the compressed air inlet. The air compressor is used for supplying compressed air into the reaction unit. On the one hand, air plays a role in stirring the reaction feed liquid. On the other hand, the oxidant generated by the reaction can also be mixed with air supplied by an air compressor to facilitate the discharge of the oxidant from the reaction unit. This is because the oxidizing agent has a certain solubility in the reaction feed liquid, and after being aerated into the reaction unit by the air compressor, the oxidizing agent can be blown out from the reaction feed liquid. The oxidant of the utility model can be gas at normal temperature. The air compressor may be disposed adjacent to the reaction unit.
In certain embodiments, the top of the reaction unit is provided with a conditioning air inlet. A blower is connected to the conditioning air inlet to blow air into the reaction unit to adjust the oxidant concentration in the mixture of air and oxidant to obtain an oxidant-containing mixed gas. By controlling the concentration of the oxidizing agent in the mixed gas, the danger caused by the excessively high concentration of the oxidizing agent such as chlorine dioxide can be avoided. Therefore, the active material producing apparatus of the present invention has high operational safety.
In certain embodiments, the top of the reaction unit is provided with a mixed gas outlet to discharge a mixed gas containing an oxidant. Further preferably, an oxidant concentration detection device is provided at the mixed gas outlet for detecting the concentration of the oxidant. The oxidizing agent concentration detection means is not particularly limited, and those known in the art may be employed.
According to an embodiment of the present invention, the reaction unit is a horizontal advection multistage reaction unit. At least one partition is arranged in the reaction unit and used for dividing the inner space of the reaction unit into a plurality of compartments. In these compartments, at least a portion of the compartments are provided with a catalyst for catalyzing the reaction feed to obtain an oxidant. Preferably, all compartments are provided with catalyst. The catalyst is preferably a honeycomb catalyst. According to the utility model discloses a concrete embodiment, set up 3 ~ 8 compartments in the reaction unit. This is advantageous in improving the reaction efficiency.
A baffling pipe may be disposed between the compartments for overflowing reaction feed from a previous compartment to a next compartment. The baffle pipe is not arranged between the compartments, and the reaction liquid in the previous compartment overflows to the next compartment through the partition.
According to an embodiment of the present invention, at least a part of the compartments of the reaction unit has a catalyst fixing position for fixing the catalyst. According to another embodiment of the present invention, all compartments of the reaction unit have catalyst-fixing sites.
The reaction unit of the utility model can be also provided with a steam inlet for supplying steam for heating to the reaction unit. According to an embodiment of the present invention, the bottom of the reaction unit is provided with a steam inlet. An outlet of the steam heater is connected to the steam inlet for providing steam for heating the reaction feed liquid in the reaction unit. The steam heater may be disposed in the vicinity of the reaction unit. The steam heater is one or more. This ensures that the reaction temperature is within a certain range.
The utility model discloses an oxidant generating equipment can also include the draught fan, and it links to each other with the mist export for carry the mist that contains the oxidant to plasma excitation equipment. The induced draft fan is respectively connected with the reaction unit and the plasma excitation equipment. Preferably, the reaction unit maintains negative pressure of-1 to-5 kPa in the reaction unit under the suction of the induced draft fan. More preferably, the negative pressure inside the reaction unit is-1.2 to-3.5 kPa. This is advantageous for forming a mixed gas containing the oxidizing agent at a certain concentration.
The utility model discloses an oxidant generating equipment can also be including the first material supply apparatus who holds material A, the second material supply apparatus who holds material C, the third material supply apparatus who holds material B and the fourth material supply apparatus who holds material S. The utility model discloses an oxidant generating equipment can also include first feed pump, second feed pump, third feed pump and fourth feed pump. The first material supply device, the second material supply device, the third material supply device and the fourth material supply device convey the material a, the material C, the material B and the material S to the reaction unit through the first supply pump, the second supply pump, the third supply pump and the fourth supply pump.
According to an embodiment of the invention, the first material supply device contains as material a slurry containing alkali metal chlorate and/or alkali metal chlorite; the second material supply device contains hydrogen peroxide and/or methanol as material C; the third material supply device contains concentrated hydrochloric acid and/or concentrated sulfuric acid as material B; the fourth material supply apparatus contains urea, sodium humate and/or sodium citrate as material S.
The utility model discloses a be provided with a plurality of feed inlets on the lateral wall of reaction unit. The first material supplying device, the second material supplying device, the third material supplying device and the fourth material supplying device are respectively connected with the feed ports, so that the material A, the material C, the material B and the material S are supplied to the reaction unit.
In some embodiments, the side wall of the reaction unit of the present invention is provided with a first feed port, a second feed port, a third feed port, and a fourth feed port. The first material supply device, the second material supply device, the third material supply device and the fourth material supply device are respectively connected with the first feed port, the second feed port, the third feed port and the fourth feed port through the first supply pump, the second supply pump, the third supply pump and the fourth supply pump so as to respectively supply the material A, the material C, the material B and the material S into the reaction unit.
In other embodiments, the reaction unit is provided with a first feed port, a second feed port, and a third feed port on a sidewall thereof. The first material supply device and the second material supply device supply materials A and C through a first supply pump and a second supply pump respectively. And the material A and the material C are mixed and then are supplied to the reaction unit through the first feeding hole. The third material supply device is connected to the second feed port by a third feed pump to supply the material B to the reaction unit. The fourth material supplying device is connected to the third feed port through a fourth supplying pump to supply the material S to the reaction unit.
The utility model discloses an oxidant generating equipment can also include mother liquor circulating equipment. The mother liquor circulating equipment comprises a mother liquor tank and a mother liquor pump. The mother liquor tank is provided with a mother liquor inlet and a mother liquor outlet. And the upper part of the reaction unit is provided with a feed liquid outlet, and the feed liquid outlet is connected with the mother liquid inlet so as to lead at least part of reaction feed liquid out to the mother liquid tank. The mother liquor may include a reflux liquid during the reaction and a mother liquor after discharging a mixed gas containing an oxidizing agent. The mother liquor outlet is connected with the reaction unit through a mother liquor pump. The reaction unit is provided with a feed liquid inlet; and the feed liquid inlet is connected with the mother liquid pump and used for circulating the mother liquid in the mother liquid tank to the reaction unit. Therefore, the recycling of the mother liquor can be realized, and the resource waste is reduced. In certain embodiments, feed B from the third feed supply is mixed with mother liquor and then fed to the reaction unit.
Plasma excitation apparatus
The utility model discloses a plasma excitation equipment includes plasma generator and high voltage power supply. The plasma generator is preferably a pulsed discharge plasma generator. The plasma generator is used for receiving the mixed gas containing the oxidant from the reaction unit, and further exciting the oxidant to form active substances under the action of the high-voltage power supply so as to form the gas containing the active substances. The active material includes active particles such as activated electrons, free radicals and the like. These active substances can oxidize NO to readily absorbable NO2Or N2O5And nitrogen oxides with high valence states.
The plasma generator is connected with the oxidation equipment so as to convey the formed gas containing active substances into the oxidation equipment, and further oxidize nitrogen oxides in the flue gas to be treated.
Flue gas denitration device
The utility model discloses a flue gas denitration device includes that above-mentioned active material produces device, oxidation equipment, nitrogen oxide absorption equipment, dust removal and discharging equipment. The active substance generating device is described in detail above and will not be described in further detail here. The oxidation apparatus, the nitrogen oxide absorption apparatus, and the dust removal and discharge apparatus will be described in detail below.
Oxidation apparatus
The utility model discloses an oxidation equipment links to each other with plasma generator to set up to can mix the gas that contains active material and pending flue gas, in order to form the flue gas after the oxidation. The gas containing the active species comes from a plasma generator. The oxidation device comprises a flue gas oxidation unit. The plasma generator is connected with the flue gas oxidation unit.
The utility model discloses a pending flue gas comes from the waste gas of steel industry. The flue gas to be treated can be flue gas from a sintering machine, pellets or a kiln. Nitrogen Oxides (NO) in flue gases to be treatedx) The content is more than or equal to 100mg/Nm3Preferably 100mg/Nm3～ 1000mg/Nm3More preferably 100mg/Nm3～300mg/Nm3. The temperature of the flue gas to be treated can be 100-150 ℃. The sulfur dioxide content may be 700mg/Nm3～ 2000mg/Nm3. The oxygen content may be 10 to 20 vol%.
The active substance can oxidize the low-valence nitrogen oxide in the smoke to be treated into the high-valence nitrogen oxide, so that oxidized smoke is formed. According to an embodiment of the present invention, the contact time of the gas containing the active material and the flue gas to be treated in the flue gas oxidation unit of the oxidation apparatus is 0.5 to 2 seconds. This is favorable to improving denitration efficiency.
Nitrogen oxide absorption equipment
The utility model discloses a nitrogen oxide absorption equipment links to each other with oxidation equipment to set up to carry out denitration treatment with the flue gas after the denitration in order to form the flue gas after the denitration with the flue gas after the oxidation. The nitrogen oxide absorption equipment comprises an absorbent bin, an absorption tower and water supply equipment. The absorbent bin is used for supplying absorbent into the absorption tower. The absorption tower is used for receiving the oxidized flue gas and the absorbent from the absorbent bin, and mixing and reacting the oxidized flue gas and the absorbent to form the denitrated flue gas. Preferably, the absorption tower is a circulating fluidized bed absorption tower. The bottom of the absorption tower is provided with a flue gas inlet. The top or the upper part of the absorption tower is provided with a flue gas outlet. The oxidation device is connected with the flue gas inlet so as to convey the oxidized flue gas to the absorption tower. An absorbent inlet is arranged above the flue gas inlet. The absorbent bin supplies powdery absorbent into the absorption tower through the absorbent inlet. The oxidized flue gas is mixed with an absorbent to form a mixed flue gas. A process water inlet is also arranged above the absorbent inlet. The water supply device is connected with the process water inlet through the water supply port, so that water is sprayed to the absorption tower to humidify the mixed flue gas. The mixed flue gas continuously rises, and denitration is finished in the absorption tower to obtain the denitrated flue gas. This is favorable to improving denitration efficiency.
Dust removal and discharge equipment
The utility model discloses a flue gas denitration device still includes dust removal and discharging equipment for purify the flue gas after the denitration in order to form the purification flue gas. The dust removing and discharging equipment comprises a bag-type dust remover, a byproduct bin and a chimney.
The bag-type dust collector is connected with the smoke outlet of the absorption tower. The bag-type dust collector is connected with the chimney. The lower part of the bag-type dust collector is connected with the byproduct bin. And discharging the denitrated flue gas from a flue gas outlet and feeding the denitrated flue gas into a bag-type dust collector. And the cloth bag dust remover removes dust from the denitrated flue gas to form purified flue gas and ash. Discharging the obtained purified flue gas from a chimney; one part of the obtained ash is conveyed to a byproduct bin, and the other part of the obtained ash is recycled to the absorption tower. The ash slag is an absorption product containing nitrate and nitrite. According to the utility model discloses an embodiment, the sack cleaner is used for purifying the flue gas after the denitration to form and purify flue gas and lime-ash. The byproduct bin is used for receiving ash from the bag-type dust collector. The chimney is used for receiving the purified flue gas from the bag-type dust remover and discharging the purified flue gas.
Introduce below and utilize the utility model discloses an above-mentioned flue gas denitration device carries out flue gas denitration method of denitration to the flue gas, including following step: 1) an oxidant forming step, 2) an active substance forming step, 3) a flue gas oxidation step and 4) an absorption step. Optionally, the flue gas denitration method of the utility model further comprises 5) a dust removal step. As described in detail below.
Step of forming an oxidizing agent
Placing a material R serving as a catalyst in a reaction unit, conveying a material A, a material B, a material C and a material S into the reaction unit through a first material supply device, a third material supply device, a second material supply device and a fourth material supply device to form a reaction material liquid, and conveying compressed air into the reaction material liquid of the reaction unit by an air compressor to perform aeration so as to promote the reaction material liquid to generate chlorine dioxide gas serving as an oxidant; the blower delivers conditioning air to the vicinity of the mixed gas outlet of the reaction unit to adjust the chlorine dioxide concentration in the mixture of air and oxidant to obtain the oxidant-containing mixed gas. The material R may be fixed at a catalyst fixing position located in the compartment.
The material A is selected from a slurry containing alkali metal chlorate and/or alkali metal chlorite. The alkali metal is sodium or potassium, preferably sodium. The concentration of alkali metal chlorate and/or alkali metal chlorite in the slurry containing alkali metal chlorate and/or alkali metal chlorite can be 200-800 g/L, preferably 210-780 g/L, and more preferably 220-750 g/L. The material B is concentrated sulfuric acid or concentrated hydrochloric acid. The material C is selected from one or two of hydrogen peroxide and methanol. The material S is selected from one or more of urea, sodium humate and sodium citrate. The material S is a stabilizer. The material R is selected from one or more of iron, manganese and cerium metal oxides.
According to one embodiment of the present invention, material a is a slurry containing sodium chlorate or a slurry containing sodium chlorite, material B is concentrated sulfuric acid or concentrated hydrochloric acid, material C is hydrogen peroxide or methanol, material R is selected from one of iron, manganese, cerium metal oxides, and material S is urea, sodium humate or sodium citrate. According to a preferred embodiment of the present invention, material a is a slurry containing sodium chlorate, material B is concentrated sulfuric acid, material C is hydrogen peroxide, material R is ferric oxide, and material S is urea. Wherein, the concentration of the concentrated sulfuric acid can be 80-99.9 wt%, preferably more than 98 wt%. The concentration of the hydrogen peroxide is 15-35 wt%, and preferably 20-30 wt%.
The feed R is preferably a honeycomb catalyst. The honeycomb catalyst is first arranged in a catalyst-retaining position in a compartment within the reaction unit. The position where the catalyst is fixed in the compartment is not particularly limited, and is preferably provided at the bottom of the reaction unit.
In certain embodiments, when the material A and the material B are added into the reaction unit, the concentration of the material A is 200-800 g/L, and the acidity of the reaction feed liquid is 4-9N, the material C and the material S are added into the reaction unit for reaction. Preferably, when the concentration of the material A is 210-780 g/L and the acidity of the reaction feed liquid is 4.2-8.6N, adding the material C and the material S into the reaction unit for reaction. More preferably, when the concentration of the material A is 220-750 g/L and the acidity of the reaction material liquid is 4.5-8.5N, adding the material C and the material S into the reaction unit to form the reaction material liquid, and reacting to obtain the oxidant.
The weight ratio of the alkali metal chlorate and/or alkali metal chlorite in the material A, the material B, the material C, the material R and the material S can be (0.9-14) to (0.6-10) to (0.8-11): (0.0002 to 0.008): (0.01 to 0.1), preferably (1.0 to 13): (0.85 to 10): 0.9 to 10): (0.0004 to 0.007): (0.015 to 0.09), more preferably (1.1 to 13): 0.75 to 9.6): 0.95 to 9.8): (0.001-0.007) and (0.015-0.08). This is advantageous for obtaining an oxidizing agent with a suitable concentration, and further, for exciting the plasma generator, thereby obtaining a highly active substance.
The reaction temperature in the reaction unit can be 50-75 ℃, preferably 50-70 ℃, and more preferably 55-70 ℃. The reaction time can be 2-8 h, preferably 2-7.5 h, and more preferably 3-7 h. This is advantageous for obtaining an oxidizing agent of suitable concentration, thereby improving the operational safety.
In the utility model, an air compressor can be used for providing compressed air to the reaction material liquid in the reaction unit to promote the generation of the oxidant; and the mixed gas containing the oxidant may be formed by supplying conditioning air to the vicinity of the mixed gas outlet of the reaction unit by a blower to adjust the concentration of the oxidant in the mixture of the air and the oxidant. This improves the operational safety.
The oxidant of the utility model can be chlorine dioxide. The mixed gas containing the oxidant may be a mixed gas containing the oxidant and air. The mixed gas containing an oxidant has an oxidant concentration of 1.5 to 5.5 vol%, preferably 1.7 to 5.2 vol%, and more preferably 2 to 5 vol%. Thus, the denitration efficiency is improved, and the operation safety is improved.
Active material formation step
And exciting the mixed gas containing the oxidant by using a plasma excitation device to form a gas containing the active substances. According to an embodiment of the present invention, the plasma generator converts the mixed gas containing the oxidant into the gas containing the active material under the action of the high voltage power supply. The plasma generator can excite an oxidant (such as chlorine dioxide) to generate active substances with high activity. The active material may include oxygen reactive ions, reactive electrons, such as ClO2·、HO·、HO2·、O3And the like. These active substances can oxidize nitrogen oxides in a lower valence state such as NO to NO which is easily absorbed2Or N2O5And nitrogen oxides with high valence states. By analyzing the components of different nitrogen oxides after oxidation, the main oxidation product is NO2、HNO3。HNO3In the form of nitric acid vapour. The utility model discloses discover, here obtain higher denitration efficiency, the operation security is also high. The plasma generator may employ process parameters conventional in the art and will not be described in detail herein.
Step of oxidizing flue gas
And introducing the gas containing the active substances into an oxidation device, and oxidizing nitrogen oxides in the flue gas to be treated to form oxidized flue gas. Gas containing active substances enters the oxidation equipment from the plasma excitation equipment, and the flue gas to be treated also enters the oxidation equipment. The gas containing the active substance and the flue gas to be treated are mixed together. The active substance oxidizes the low-valence nitrogen oxide in the flue gas to be treated into the high-valence nitrogen oxide, so that oxidized flue gas is formed.
The flue gas to be treated of the utility model can be flue gas from a sintering machine, pellets or a kiln. Nitrogen Oxides (NO) in flue gases to be treatedx) The content is more than or equal to 100mg/Nm3Preferably 100mg/Nm3～1000mg/Nm3More preferably 100mg/Nm3～ 300mg/Nm3. The temperature of the flue gas to be treated can be 100-150 ℃. The sulfur dioxide content may be 700mg/Nm3～2000mg/Nm3. Oxygen gasThe gas content may be 10 to 20 vol%.
The contact time of the active substance and the flue gas to be treated in the oxidation equipment is 0.5-2 s, preferably 0.6-2 s, and more preferably 0.8-1.8 s. The flow speed of the flue gas to be treated is less than 20m/s, preferably 1-20 m/s, and more preferably 2-15 m/s. The nitrogen oxides in the higher valence state are easily absorbed. The utility model discloses avoid directly letting in the plasma reaction unit with the flue gas to improve the operation security.
Absorption step
And introducing the oxidized flue gas into nitrogen oxide absorption equipment, and absorbing by using a powdery absorbent to form the denitrated flue gas. The nitrogen oxide absorption equipment comprises an absorption tower, an absorbent bin and water supply equipment. According to the utility model discloses an embodiment lets in the absorption tower with the flue gas after the oxidation, carries the likepowder absorbent in the future from absorbent storehouse to in the absorption tower to mix in order to form mixed flue gas with the flue gas after the oxidation. And water is sprayed into the absorption tower by the water supply equipment to humidify the mixed flue gas, so that denitration is finished in the absorption tower, and the denitrated flue gas is obtained.
The absorbent may be selected from one or more of calcium oxide, calcium hydroxide, magnesium oxide, magnesium hydroxide, sodium carbonate, sodium bicarbonate and fly ash. Preferably, the absorbent is selected from one or more of calcium hydroxide, magnesium hydroxide, sodium carbonate, sodium bicarbonate and fly ash. More preferably, the absorbent is calcium hydroxide and fly ash absorbent. Wherein the mass ratio of the calcium hydroxide to the fly ash is 1-5: 1, preferably 1.2-4.5: 1, and more preferably 1.5-3.5: 1.
The absorption column is preferably a circulating fluidized bed absorption column. The oxidized flue gas is fully and uniformly mixed with the absorbent in the circulating fluidized bed absorption tower, and meanwhile, a proper amount of process water is sprayed to generate nitrate and nitrite, so that the denitration effect is achieved. Through the multiple circulation of the absorbent, the contact time of the absorbent and the oxidized smoke is prolonged, and the utilization rate of the absorbent is improved.
Dust removal step
And introducing the denitrated flue gas into a bag-type dust collector to form purified flue gas and ash. The purified flue gas is discharged from a chimney. And conveying a part of denitration byproducts in the ash residues to the absorption tower again to realize recycling. And conveying the other part of denitration byproducts in the ash to a byproduct bin.
The present invention will be described in more detail with reference to the accompanying drawings and examples.
The starting materials for the following examples are illustrated below:
an absorbent: the absorbent is formed by calcium hydroxide and fly ash, and the mass ratio of the calcium hydroxide to the fly ash is 3: 1.
Concentrated sulfuric acid: 98 wt%.
Hydrogen peroxide: 27 wt%.
Slurry containing sodium chlorate: is formed by dispersing sodium chlorate solid in water, and the concentration is 560 g/L.
Example 1
Fig. 1 is a schematic structural view of an active material generating apparatus including a plasma generating device according to the present invention. The active material generating apparatus includes an oxidant generating device 100 and a plasma excitation device 200.
The oxidant generation device 100 includes a first material supply device 1 containing a material a, a second material supply device 2 containing a material C, a third material supply device 3 containing a material B, and a fourth material supply device 4 containing a material S. The oxidant generation apparatus 100 further includes a first feed pump 6, a second feed pump 7, a third feed pump 8, a fourth feed pump 9, a reaction unit 10, a steam inlet 11, an air supply unit, a mother liquor circulation apparatus, and an induced draft fan 16. The air supply unit includes a blower 12 and an air compressor 13.
The reaction unit 10 of this example is a horizontal, parallel flow reactor. The reaction unit 10 is partitioned into a plurality of compartments by partitions. A baffling pipe is arranged between the compartments. The reaction liquid in the previous compartment overflows to the next compartment through the baffled pipe. At least a part of the compartments have catalyst fixing sites 5 for fixing the material R (honeycomb catalyst).
The bottom of the reaction unit 10 is provided with a steam inlet 11 to supply steam for heating into the reaction unit 10. The steam may be generated by one or more steam generators.
The side wall of the reaction unit 10 is provided with a first feed opening, a second feed opening, and a third feed opening (not shown). The first material supply apparatus 1 and the second material supply apparatus 2 supply the material a and the material C by a first supply pump 6 and a second supply pump 7, respectively. The material a and the material C are mixed and then supplied to the reaction unit 10 through the first feed port. The third material supplying device 3 is connected to the second feed port by a third feed pump 8 to supply the material B to the reaction unit 10. The fourth material supplying device 4 is connected to the third feed port by a fourth supply pump 9 to supply the material S to the reaction unit 10. This forms the reaction feed.
A compressed air inlet (not shown) is provided at an upper portion of a sidewall of the reaction unit 10, and an air compressor 13 is connected to the compressed air inlet to supply compressed air to the reaction feed liquid of the reaction unit 10 for aeration, thereby functioning to stir the reaction feed liquid. The air and the oxidizing agent form a mixture.
An air inlet for conditioning (not shown) is provided at the top of the reaction unit 10. A blower 12 is connected to the conditioning air inlet to blow conditioning air near the mixed gas outlet of the reaction unit 10 to adjust the oxidant concentration in the mixture of air and oxidant to form a mixed gas containing oxidant. An oxidizing agent concentration detector (not shown) is preferably provided at the mixed gas outlet at the top of the reaction unit.
The top of the reaction unit 10 is provided with a mixed gas outlet (not shown). The mixed gas outlet is connected with an induced draft fan 16, and the induced draft fan 16 is connected with a plasma generator 17. The mixed gas containing the oxidant is sent to the plasma generator 17 by the action of the induced draft fan 16.
The upper part of the reaction unit 10 is also provided with a feed liquid outlet. The mother liquor circulating device comprises a mother liquor tank 14 and a mother liquor pump 15. The mother liquor tank 14 is provided with a mother liquor inlet and a mother liquor outlet. The mother liquor inlet is connected to the feed liquor outlet to direct a portion of the reaction feed liquor to the mother liquor tank 14. The mother liquor tank 14 is connected to the second feed port via a mother liquor pump 15, and the mother liquor in the mother liquor tank 14 is mixed with the material B of the third material supply device 3 and then conveyed to the reaction unit 10.
The plasma excitation apparatus 200 includes a plasma generator 17 and a high voltage power supply. The high voltage power supply is used to supply power to the plasma generator 17. The plasma generator 17 of the present embodiment is preferably a pulse discharge plasma generator. The plasma generator 17 further excites the mixed gas containing the oxidizing agent by a high-voltage power supply (not shown) to form a gas containing active substances.
In the practice, the feed A is preferably a slurry containing alkali metal chlorate or a slurry containing alkali metal chlorite. The material C is preferably hydrogen peroxide or methanol. The material B is preferably concentrated hydrochloric acid or concentrated sulfuric acid. The material S is preferably urea, sodium humate or sodium citrate. The material R is a honeycomb transition metal oxide catalyst which may be selected from iron oxide, manganese oxide or cerium oxide.
Example 2
Fig. 2 shows a schematic structural diagram of a flue gas denitration device of the utility model. The flue gas denitration apparatus of the present embodiment includes the active material generating apparatus of embodiment 1, the oxidizing device 300, the nitrogen oxide absorbing device 400, and the dust removing and discharging device 500.
The oxidation plant 300 comprises a flue gas oxidation unit 18. The plasma generator 17 is connected to a flue gas oxidation unit 18. The gas containing active substances is conveyed from the plasma generator 17 to the flue gas oxidation unit 18, and the nitrogen oxides in the flue gas to be treated are oxidized to obtain oxidized flue gas.
The nitrogen oxide absorption apparatus 400 includes an absorbent bin 19, a water supply apparatus 20, and an absorption tower 21. The absorption tower 21 of this embodiment is a circulating fluidized bed absorption tower. The bottom of the absorber 21 has a flue gas inlet (not shown). The flue gas oxidation unit 18 is connected to the flue gas inlet to deliver the oxidized flue gas to the absorber tower 21. An absorbent inlet (not shown) is provided above the flue gas inlet. The absorbent bin 19 supplies absorbent into the absorption tower 21 through an absorbent inlet. The oxidized flue gas is mixed with an absorbent to form a mixed flue gas. A water supply port is also arranged above the absorbent inlet. The water supply device 20 sprays water to the absorption tower 21 through the water supply port to humidify the mixed flue gas. The mixed flue gas continuously rises, and denitration is completed in the absorption tower 21 to obtain the denitrated flue gas.
The top of the absorber 21 is provided with a flue gas outlet (not shown). The dust-removing and discharging device 500 includes a bag-type dust collector 22, a byproduct bin 23, and a stack 24. The bag-type dust collector 22 is connected with the flue gas outlet of the absorption tower 21. The bag-type dust collector 22 is connected with the chimney 24. The lower part of the bag-type dust collector 22 is connected with a byproduct bin 23. The denitrated flue gas is discharged from the flue gas outlet and enters the bag-type dust collector 22. The bag-type dust collector 22 removes dust from the denitrated flue gas to obtain purified flue gas and ash. The cleaned flue gas is discharged from the stack 24. A part of the ash is transferred to the by-product bin 23 and the other part is recycled to the absorption tower 21.
Example 3
The same as example 2 except for the following settings:
all compartments have catalyst fixing sites 5 for fixing the material R (honeycomb catalyst).
Example 4
The flue gas denitration device of example 3 was used for an 80 ten thousand ton/a pellet denitration project.
The honeycomb catalyst iron sesquioxide (material R) is fixed to the catalyst fixing site 5 in the compartment of the reaction unit 10. Slurry containing sodium chlorate (material A), concentrated sulfuric acid (material B), hydrogen peroxide (material C) and urea (material S) are conveyed into a reaction unit 10 to form reaction feed liquid.
The reaction unit 10 adopts a horizontal advection multistage reaction unit, 4 compartments are arranged in the reaction unit, and each compartment overflows to the next compartment by adopting a baffling pipe. Steam is supplied to the reaction unit 10 through the steam inlet 11 to heat the reaction feed liquid. Compressed air from an air compressor 13 is blown into the reaction liquid of the reaction unit for aeration, and the generated chlorine dioxide and air form a mixture. The concentration of chlorine dioxide in the mixture was adjusted to 3 vol% by blowing conditioning air by a blower 12, and a mixed gas containing an oxidant was obtained and discharged from the reaction unit 10. The mixed gas containing the oxidant is delivered to a plasma generator 17 under the action of an induced draft fan 16.
The mixed gas containing the oxidant is converted into a gas containing the active material by the plasma generator 17.
The gas containing the active species is transported from the plasma generator 17 to the flue gas oxidation unit 18. The gas containing the active substance is mixed with the flue gas to be treated. The active substance oxidizes the low-valence nitrogen oxide in the flue gas to be treated into the high-valence nitrogen oxide, so that oxidized flue gas is formed. The contact time of the gas containing the active substances and the flue gas to be treated in the flue gas oxidation unit 18 is 2 s.
And introducing the oxidized flue gas into an absorption tower 21, conveying an absorbent containing calcium hydroxide and fly ash from an absorbent bin 19 into the absorption tower 21, and mixing the absorbent with the oxidized flue gas to form mixed flue gas. The water supply device 20 sprays water into the absorption tower 21 to humidify the mixed flue gas. The absorbent absorbs the high-valence nitrogen oxide in the oxidized flue gas to form denitrated flue gas.
And introducing the denitrated flue gas into a bag-type dust collector 22 to form purified flue gas and ash. The cleaned flue gas is discharged from a stack 24. A part of the ash is conveyed to the absorption tower 21 for recycling. Another portion of the ash is conveyed to the by-product bin 23.
The main process parameters and results are detailed in tables 1, 2 and 3. In this example, the yield of chlorine dioxide was 1 t/d. By analyzing the components of different nitrogen oxides after oxidation, the oxidation rate of NO is 88 percent, and the nitrogen oxides are mainly oxidized into NO2、HNO3Wherein HNO3In the form of nitric acid vapour. The operation is carried out for 12 months, and the operation safety is high.
TABLE 1 flue gas parameters to be treated
| Parameter(s) | Unit of | Numerical value | |
| Flue gas volume (working condition) | m3/h | 480000 | |
| Standard flue gas volume | Nm3/h | 320000 | |
| Inlet NOx concentration | mg/Nm3 | 150 | |
| Dust at the inlet | mg/ |
110 | |
| Temperature of | ℃ | 110 | |
| Moisture content of flue gas | ％ | 17.4 |
TABLE 2
| Name of raw materials | Dosage (parts by weight) |
| Sodium chlorate in slurry (A) containing sodium chlorate | 1.3 |
| Concentrated sulfuric acid (B) | 0.9 |
| Hydrogen peroxide (C) | 1.1 |
| Iron oxide (R) | 0.001 |
| Urea (S) | 0.02 |
TABLE 3
| Parameter(s) | Unit of | Numerical value |
| Outlet flue gas volume (working condition) | m3/h | 520000 |
| Standard flue gas volume | Nm3/h | 365000 |
| Outlet NOx concentration | mg/ |
20 |
| Dust at the outlet | mg/Nm3 | 1 |
| Temperature of flue gas | ℃ | 95 |
| Denitration efficiency | ％ | 87 |
Example 5
The flue gas denitration device of example 3 was used for 162m2And 4, denitration items of the sintering machine. The difference from example 4 is the amount of raw material and the flue gas parameters.
The main process parameters and results are detailed in tables 4, 5 and 6. In this example, the yield of chlorine dioxide was 3.5 t/d. By analyzing the components of different nitrogen oxides after oxidation, the oxidation rate of NO is 90%. The operation is carried out for 12 months, and the operation safety is high.
TABLE 4 flue gas parameters to be treated
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 960000 |
| Standard flue gas volume | Nm3/h | 650000 |
| Inlet NOx concentration | mg/Nm3 | 220 |
| Dust at the inlet | mg/Nm3 | 45 |
| Temperature of flue gas | ℃ | 130 |
| Moisture content of flue gas | ％ | 16.4 |
TABLE 5
| Name (R) | Dosage (parts by weight) |
| Sodium chlorate in slurry (A) containing sodium chlorate | 6.9 |
| Concentrated sulfuric acid (B) | 5.0 |
| Hydrogen peroxide (C) | 5.2 |
| Iron oxide (R) | 0.003 |
| Urea (S) | 0.05 |
TABLE 6
| Parameter(s) | Unit of | Numerical value |
| Outlet flue gas volume (working condition) | m3/h | 1010000 |
| Standard flue gas volume | Nm3/h | 720000 |
| Outlet NOx concentration | mg/Nm3 | 30 |
| Dust at the outlet | mg/Nm3 | 1 |
| Temperature of flue gas | ℃ | 95 |
| Denitration efficiency | ％ | 86 |
Example 6
The flue gas denitration device of the embodiment 3 is used for 265m2And 4, denitration items of the sintering machine. The difference from example 4 is the amount of raw material and the flue gas parameters. The chlorine dioxide concentration in the mixed gas containing chlorine dioxide was 5 vol%.
The main process parameters and results are detailed in table 7, table 8 and table 9. In this example, the yield of chlorine dioxide was 7.5 t/d. By analyzing the components of different nitrogen oxides after oxidation, the oxidation rate of NO is 92%. The operation is carried out for 12 months, and the operation safety is high.
TABLE 7 flue gas parameters to be treated
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 1590000 |
| Standard flue gas volume | Nm3/h | 1070000 |
| Inlet NOx concentration | mg/Nm3 | 300 |
| Dust at the inlet | mg/Nm3 | 45 |
| Temperature of flue gas | ℃ | 130 |
| Moisture content of flue gas | ％ | 16.4 |
TABLE 8
| Name (R) | Dosage (parts by weight) |
| Sodium chlorate in slurry (A) containing sodium chlorate | 12.8 |
| Concentrated sulfuric acid (B) | 9.2 |
| Hydrogen peroxide (C) | 9.6 |
| Iron oxide (R) | 0.007 |
| Urea (S) | 0.08 |
TABLE 9
| Parameter(s) | Unit of | Numerical value |
| Outlet flue gas volume (working condition) | m3/h | 1650000 |
| Standard flue gas volume | Nm3/h | 1170000 |
| Outlet NOx concentration | mg/Nm3 | 30 |
| Dust at the outlet | mg/Nm3 | 1 |
| Temperature of flue gas | ℃ | 95 |
| Denitration efficiency | ％ | 90 |
The present invention is not limited to the above embodiments, and any variations, modifications, and substitutions that may occur to those skilled in the art may be made without departing from the spirit of the present invention.
Claims (10)
1. An active material generating device, comprising:
an oxidant generation apparatus including an air supply unit and a reaction unit; the reaction unit is used for generating an oxidant; the air supply unit is used for supplying compressed air to the reaction liquid in the reaction unit to promote the generation of the oxidant and supplying air for adjusting to the vicinity of a mixed gas outlet of the reaction unit so as to adjust the concentration of the oxidant in a mixture formed by the air and the oxidant and form mixed gas containing the oxidant; and
a plasma excitation apparatus includes a plasma generator for exciting a mixed gas containing an oxidant to form a gas containing an active substance.
2. The active material generating apparatus according to claim 1, characterized in that:
the reaction unit is provided with a compressed air inlet and an air inlet for regulation;
the air supply unit includes an air compressor and a blower;
the air compressor is connected with the compressed air inlet and is used for blowing compressed air into the reaction liquid of the reaction unit so as to promote the generation of an oxidant;
the blower is connected with the regulating air inlet and used for supplying regulating air to the vicinity of the mixed gas outlet of the reaction unit so as to regulate the concentration of the oxidant in the mixture formed by the air and the oxidant and form mixed gas containing the oxidant.
3. The active material producing device according to claim 2, wherein the reaction unit is a horizontal advection multistage reactor, at least one partition is provided in the reaction unit, and the partition is used for dividing an inner space of the reaction unit into a plurality of compartments; in these compartments, at least a part of the compartments are provided with a catalyst for catalyzing the reaction feed to obtain an oxidant; wherein the catalyst is a honeycomb catalyst.
4. The active material producing device according to claim 3, wherein a baffle pipe for overflowing the reaction liquid of a preceding compartment to a next compartment is provided between the compartments.
5. The active material generating apparatus according to claim 4, wherein:
the reaction unit is also provided with a steam inlet which is arranged to supply steam for heating to the reaction unit;
the oxidant generating equipment also comprises a draught fan which is connected with the mixed gas outlet and used for conveying the mixed gas containing the oxidant to the plasma excitation equipment.
6. The active material producing device according to claim 5, wherein the oxidant generating means further includes mother liquor circulating means including a mother liquor tank and a mother liquor pump; the mother liquor tank is provided with a mother liquor inlet and a mother liquor outlet; the mother liquor outlet is connected with the mother liquor pump;
the reaction unit is provided with a feed liquid outlet; the feed liquid outlet is connected with the mother liquid inlet, so that at least one part of reaction feed liquid is led out to a mother liquid tank;
the reaction unit is also provided with a feed liquid inlet; and the feed liquid inlet is connected with the mother liquid pump and used for circulating the mother liquid in the mother liquid tank to the reaction unit.
7. The active material producing device according to claim 6, wherein the oxidant generating means further includes first material supplying means containing a material A, second material supplying means containing a material C, third material supplying means containing a material B, and fourth material supplying means containing a material S;
a plurality of feed inlets are formed in the side wall of the reaction unit;
the first material supply device, the second material supply device, the third material supply device and the fourth material supply device are respectively arranged to be capable of being connected with the feed ports so as to supply the material A, the material C, the material B and the material S to the reaction unit.
8. A flue gas denitration device is characterized by comprising:
an active material generating apparatus according to any one of claims 1 to 7; and
the oxidation device is connected with the plasma generator and is arranged to mix the gas containing the active substances and the flue gas to be treated so as to form oxidized flue gas; and
and the nitrogen oxide absorption equipment is connected with the oxidation equipment and is set to be capable of carrying out denitration treatment on the oxidized flue gas so as to form denitrated flue gas.
9. The flue gas denitration device according to claim 8, wherein the nitrogen oxide absorption equipment comprises an absorption tower, an absorbent bin and water supply equipment; the absorption tower is a circulating fluidized bed absorption tower; the absorption tower is provided with a flue gas inlet and a flue gas outlet; the oxidation equipment is connected with the flue gas inlet and is arranged to convey the oxidized flue gas to the absorption tower; the absorbent bin is connected with the absorption tower and is arranged to supply powdery absorbent to the absorption tower; the water supply device is arranged to spray water into the absorption tower so as to humidify the absorbent and the oxidized flue gas.
10. The flue gas denitration apparatus according to claim 9, further comprising a dust removal and discharge device connected to the nitrogen oxide absorption device, for treating the denitrated flue gas into a purified flue gas and discharging the purified flue gas.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111167278A (en) * | 2020-03-02 | 2020-05-19 | 中晶蓝实业集团有限公司 | Flue gas denitration device and method containing plasma generation equipment |
| CN114028925A (en) * | 2021-05-27 | 2022-02-11 | 苏州仕净环保科技股份有限公司 | Desulfurization and denitrification agent for flue gas and desulfurization and denitrification method and device thereof |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111167278A (en) * | 2020-03-02 | 2020-05-19 | 中晶蓝实业集团有限公司 | Flue gas denitration device and method containing plasma generation equipment |
| CN111167278B (en) * | 2020-03-02 | 2024-01-30 | 中晶环境科技股份有限公司 | Flue gas denitration device and method containing plasma generating equipment |
| CN114028925A (en) * | 2021-05-27 | 2022-02-11 | 苏州仕净环保科技股份有限公司 | Desulfurization and denitrification agent for flue gas and desulfurization and denitrification method and device thereof |
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Effective date of registration: 20201208 Address after: 100176, Beijing Beijing Daxing District economic and Technological Development Zone ronghua South Road No. 10, Ronghua International Building No. 20, 3 floor Patentee after: Shanghui TONG Address before: 100176, Beijing Beijing Daxing District economic and Technological Development Zone ronghua South Road No. 10, Ronghua International Building No. 20, 3 floor Patentee before: Zhongjing Kunlun Industrial Group Co., Ltd |