CN211837226U - Oxidizing solution production equipment and flue gas denitration device - Google Patents
Oxidizing solution production equipment and flue gas denitration device Download PDFInfo
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- CN211837226U CN211837226U CN202020238598.9U CN202020238598U CN211837226U CN 211837226 U CN211837226 U CN 211837226U CN 202020238598 U CN202020238598 U CN 202020238598U CN 211837226 U CN211837226 U CN 211837226U
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Abstract
The utility model discloses an oxidizing solution production facility and flue gas denitrification facility. The oxidizing solution production apparatus includes a reactor for preparing an oxidizing gas by reacting a feed liquid and forming a mixed gas with air; it is provided with a compressed air inlet, an air inlet for regulation and a mixed gas outlet; an air compressor disposed in connection with the compressed air inlet for providing compressed air to the reactor; a blower connected to the conditioning air inlet for supplying conditioning air to the reactor; the mixed gas absorption device is arranged to be connected with the mixed gas outlet and is used for converting oxidizing gas in the mixed gas into a solution to form oxidizing solution and air; and the refrigerating device is arranged to be connected with the mixed gas absorption device and is used for providing the chilled water for the mixed gas absorption device. The equipment has high operation safety.
Description
Technical Field
The utility model relates to an oxidizing solution production facility and flue gas denitration device.
Background
The emission of nitrogen oxides into the air causes atmospheric pollution. As a main nitrogen oxide emission source in the steel industry, the denitration technology of the steel industry receives more and more attention. The denitration technology combining the oxidant with the absorption flue gas is a novel denitration technology, and the method oxidizes NO with low solubility in the flue gas into NO by utilizing the principle of forced oxidation2、N2O5The nitrogen oxides with high valence state are absorbed by water or alkaline substances, and the method has the advantages of low modification cost, small occupied area, simple process, strong adaptability and the like.
The chlorine dioxide is used as a green oxidant with strong oxidizability, has low cost, and has better effect when being applied to an oxidation-combined absorption method for desulfurization and denitrification. However, chlorine dioxide is extremely easy to decompose, so that the chlorine dioxide has explosion danger and is not beneficial to industrial safety application.
CN203750390U discloses a three-section flue gas desulfurization and denitration system simultaneously based on calcium base and chlorine dioxide. The desulfurization and denitrification system comprises an absorption tower, a chlorine dioxide generator, a desulfurization circulating tank, an oxidant circulating tank and a denitrification circulating tank; a smoke outlet, a dehydration demister, a denitration spray pipe, an ascending gas and liquid collecting device, an oxidation spray pipe, a descending gas and liquid collecting device, a desulfurization spray pipe and a smoke inlet are sequentially arranged in the absorption tower from top to bottom; a stirrer is arranged in the desulfurization circulating reaction tank, an oxidation air distribution pipe is arranged at the lower part of the desulfurization circulating reaction tank, the oxidation air distribution pipe is connected with a fan outside the desulfurization circulating reaction tank, and a desulfurization product at the lower part of the oxidation air distribution pipe enters a desulfurization product outlet; the chlorine dioxide generator is connected with an oxidant circulating tank, an outlet of the oxidant circulating tank is connected with an oxidation spray pipe in the absorption tower body through an oxidant circulating pump, and an inlet of the oxidant circulating tank is connected with a lower gas-raising and liquid-collecting device in the absorption tower body; an outlet of the denitration circulating tank is connected with a denitration spraying pipe in the absorption tower body through a denitration circulating pump, one inlet of the denitration circulating tank is connected with an ascending gas and liquid collecting device in the absorption tower body, the other inlet of the denitration circulating tank is connected with a denitration circulating reaction tank through a slurry conveying pump, and a denitration product at the bottom of the denitration circulating tank enters a denitration product outlet; the desulfurization spray pipe is connected with the desulfurization circulation reaction tank through a desulfurization circulating pump. The system does not disclose the specific structure of the chlorine dioxide generator, and the denitration efficiency is low.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides an oxidizing solution production facility, this equipment oxidizing gas's concentration can be adjusted, and the operational safety is high. Further, the present invention has a high oxidizing gas yield. On the other hand, the utility model provides a flue gas denitration device, the device's operational safety is high.
In one aspect, the present invention provides an oxidizing solution production apparatus, comprising:
a reactor for preparing an oxidizing gas from the reaction feed liquid and forming a mixed gas with air; it is provided with a compressed air inlet, an air inlet for regulation and a mixed gas outlet;
an air compressor disposed in connection with the compressed air inlet for providing compressed air to the reactor;
a blower connected to the conditioning air inlet for supplying conditioning air to the reactor;
the mixed gas absorption device is arranged to be connected with the mixed gas outlet and is used for converting oxidizing gas in the mixed gas into a solution to form oxidizing solution and air;
and the refrigerating device is arranged to be connected with the mixed gas absorption device and is used for providing the chilled water for the mixed gas absorption device.
According to the utility model discloses an oxidizing solution production facility, preferably, the reactor still is provided with the circulating air entry, the mist absorption equipment has the air outlet, the air outlet still links to each other with the circulating air entry for with at least a part air circulation to reactor.
According to the oxidizing solution production apparatus of the present invention, preferably, the reactor is further provided with a steam inlet for supplying steam for heating to the reactor.
In the oxidizing solution production apparatus according to the present invention, preferably, the reactor is a horizontal type parallel flow reactor; at least one partition is arranged in the reactor and can divide the inner space of the reactor into a plurality of compartments; in at least a part of the compartments, a honeycomb catalyst is provided for catalyzing the reaction feed to obtain oxidizing gases.
According to the utility model discloses an oxidizing solution production facility, 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 utility model discloses an oxidizing solution production facility, preferably, oxidizing solution production facility still includes the mother liquor jar, the mother liquor jar has mother liquor entry and mother liquor export;
the reactor 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 reactor is provided with a feed liquid inlet; the feed liquid inlet is connected with the mother liquid outlet and is configured to circulate the mother liquid in the mother liquid tank to the reactor.
According to the utility model discloses an oxidizing solution production facility, preferably, oxidizing solution production facility still includes the first head tank that contains material A, the second head tank that contains material C, the third head tank that contains material B and the fourth head tank that contains material S;
a first feed port, a second feed port, a third feed port and a fourth feed port are arranged on the side wall of the reactor; first head tank is connected with first feed inlet to supply with material A to the reactor, the second head tank is connected with the second feed inlet, thereby supply with material C to the reactor, the third head tank links to each other with the third feed inlet, thereby supply with material B to the reactor, the fourth head tank leads to and links to each other with the fourth feed inlet, thereby supplies with material S to the reactor, forms the reaction feed liquid.
According to the utility model discloses an oxidizing solution production facility, preferably, oxidizing solution production facility still includes the first head tank that contains material A, the second head tank that contains material C, the third head tank that contains material B and the fourth head tank that contains material S;
a first feeding hole, a second feeding hole and a third feeding hole are formed in the side wall of the reactor;
the first raw material tank and the second raw material tank are both arranged to be connected with the first feed inlet, so that the material A and the material C are mixed and then are fed to the reactor through the first feed inlet;
a third raw material tank is arranged to be capable of being connected with the second feed port so as to feed the material B to the reactor;
a fourth feed tank is provided connectable to the third feed port to supply material S to the reactor to form a reaction feed.
In the oxidizing solution production apparatus according to the present invention, preferably, the first raw material tank contains, as the material a, a slurry containing alkali metal chlorate and/or alkali metal chlorite;
the second raw material tank contains hydrogen peroxide and/or methanol as a material C;
the third raw material tank contains concentrated hydrochloric acid and/or concentrated sulfuric acid serving as a material B;
the fourth raw material tank contains urea, sodium humate and/or sodium citrate as the material S.
On the other hand, the utility model provides a flue gas denitration device, include:
the above oxidizing solution producing apparatus, wherein the mixed gas absorbing apparatus further has an oxidizing solution outlet and an air outlet;
the plasma generation and flue gas oxidation equipment is provided with an oxidizing atomized liquid inlet, and the oxidizing solution outlet and the air outlet are respectively connected with the oxidizing atomized liquid inlet, so that oxidizing solution and air are mixed to form oxidizing atomized liquid and then enter the plasma generation and flue gas oxidation equipment; the plasma generation and flue gas oxidation equipment is arranged to convert the oxidizing atomized liquid into liquid oxidizing ions and oxidize nitric oxides in the flue gas to be treated to form oxidized flue gas;
and the denitration device is connected with the plasma generation and flue gas oxidation device and is arranged to be capable of carrying out denitration treatment on the oxidized flue gas from the plasma generation and flue gas oxidation device so as to obtain the denitration flue gas.
The oxidizing solution production equipment of the utility model has the advantages that the concentration of the oxidizing gas can be adjusted, and the industrial application is safe. Further, the present invention has a high oxidizing gas yield. On the other hand, the utility model provides a denitrification facility, the device industrial application safety. Furthermore, the device can convert the oxidizing solution into liquid oxidizing ions, so that the oxidizing performance is improved, and the higher oxidation rate of the nitrogen oxide can be achieved in a short time.
Drawings
Fig. 1 is a schematic view of an oxidizing solution production apparatus according to the present invention.
Fig. 2 is a schematic view of another oxidizing solution production apparatus according to the present invention.
Fig. 3 is the utility model discloses a flue gas denitration device's schematic diagram.
Fig. 4 is a schematic view of another flue gas denitration device of the utility model.
The reference numerals are explained below:
1-a first feedstock tank; 2-a second feed tank; 3-a third raw material tank; 4-a fourth feed tank; 5-a catalyst; 6-a first feed pump; 7-a second feed pump; 8-a third feed pump; 9-a fourth feed pump; 10-a reactor; 11-a steam inlet; 12-a blower; 13-an air compressor; 14-mother liquor tank; 15-mother liquor pump; 16-mixed gas absorption equipment; 17-a refrigeration device; 18-chilled water; 19-a draught fan; 20-a delivery pump; 21-plasma generation and oxidation equipment; 22-an absorbent bin; 23-a water supply device; 24-a denitration absorption tower; 25-a dust remover; 26-a byproduct bin; 27-chimney.
Detailed Description
The present invention will be further described with reference to the following specific examples, but the scope of the present invention is not limited thereto.
< oxidizing solution production facility >
The utility model discloses an oxidizing solution production facility includes reactor, air compressor, air-blower, mist absorption equipment and refrigeration plant. Optionally, the utility model discloses a denitrification facility still includes mother liquor jar and/or head tank.
Reactor with a reactor shell
The reactor of the utility model is used for preparing oxidizing gas and leading the oxidizing gas and air to form mixed gas. The reactor is provided with a plurality of feed inlets, a compressed air inlet, an air inlet for regulation and a mixed gas outlet.
A plurality of feed ports are provided in communication with the plurality of feed tanks for delivering reaction feed to the reactor. According to an embodiment of the present invention, the plurality of feed inlets are provided on the side wall of the reactor.
The compressed air inlet is used for conveying compressed air to the reactor. The compressed air inlet is connected with an air compressor. According to an embodiment of the present invention, the compressed air inlet is provided at an upper portion of the sidewall of the reactor.
The adjusting air inlet is used for blowing air into the reactor, thereby adjusting the concentration of the oxidizing gas in the reactor. The regulating air inlet is connected with the blower. According to one embodiment of the invention, the conditioning air inlet is arranged at the top of the reactor.
The mixed gas outlet is used for conveying the mixed gas to the mixed gas absorption equipment. The mixed gas outlet is connected with the mixed gas absorption equipment. According to an embodiment of the present invention, the mixed gas outlet is provided at the top of the reactor.
The reactor may also be provided with a feed liquid outlet and/or a feed liquid inlet. The feed liquid outlet may be disposed in an upper portion of the reactor. The feed liquid inlet may be provided in the side wall of the reactor. The feed liquid inlet may be common to the feed inlet.
The reactor is also provided with a steam inlet for supplying heating steam to the reactor. Preferably, the steam inlet is arranged at the bottom of the reactor. Thus, heat exchange is carried out more fully, the reaction temperature is ensured, and the reaction is promoted to be carried out.
The reactor is further provided with a recycle air inlet for recycling air into the reactor. The circulating air inlet is connected with the air outlet of the mixed gas absorption device. According to one embodiment of the invention, the circulation air inlet is arranged at the top of the reactor.
The reactor of the utility model can be a horizontal type parallel flow reactor. At least one partition is disposed within the reactor. The partition is used to divide an inner space of the reactor into a plurality of compartments. According to the utility model discloses an embodiment, 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. Thus, the reaction liquid can be subjected to multi-stage reaction. According to another embodiment of the present invention, no baffling tube is provided between the compartments of the reactor, and the reaction liquid of the previous compartment overflows to the next compartment through the spacer.
In at least a part of the compartments, a honeycomb catalyst is provided for catalyzing the reaction feed to obtain oxidizing gases. According to one embodiment of the present invention, a honeycomb catalyst for catalyzing the reaction liquid to obtain the oxidizing gas is provided in all the compartments.
According to a particular embodiment of the present invention, the reactor is a horizontal, parallel flow reactor; at least one partition is arranged in the reactor and can divide the inner space of the reactor into a plurality of compartments; in at least a part of the compartments, a honeycomb catalyst is provided for catalyzing the reaction feed to obtain oxidizing gases.
Air compressor
The utility model discloses an air compressor can adopt conventional air compression equipment. An air compressor is arranged in connection with the compressed air inlet of the reactor for providing compressed air to the reactor. Specifically, an air compressor provides compressed air to the reaction feed liquid of the reactor. The compressed air is aerated in the reactor to fully stir the reaction liquid, which is beneficial to the reaction and the escape of oxidizing gas. The reaction feed liquid generates oxidizing gas, and the reactor contains oxidizing gas and air.
Blower fan
The utility model discloses an air-blower can adopt conventional air-blast equipment. The blower is connected to the conditioning air inlet of the reactor and blows conditioning air into the reactor to adjust the concentration of the oxidizing gas in the reactor to form a mixed gas. Specifically, a blower blows conditioning air to the vicinity of the mixed gas outlet of the reactor to adjust the concentration of chlorine dioxide in the mixed gas. Therefore, the concentration of chlorine dioxide in the mixed gas can be adjusted, and the danger caused by overhigh concentration of chlorine dioxide is avoided. The mixed gas is discharged from the mixed gas outlet of the reactor.
Mixed gas absorption equipment
The utility model discloses a mist absorption equipment can adopt conventional absorption tower. The mixed gas absorption device is used for converting the oxidizing gas in the mixed gas into a solution to form an oxidizing solution and air. The mixed gas absorption device is connected with the mixed gas outlet of the reactor. The mixed gas absorption equipment is also provided with a chilled water inlet, an oxidizing solution outlet and an air outlet.
The chilled water inlet is used for supplying chilled water to the mixed gas absorption device body. The chilled water inlet is connected with a refrigeration device. The frozen water is sprayed from the upper part of the mixed gas absorption device and is mixed with the mixed gas, the oxidizing gas is solid in the cold water to form oxidizing solution, and the air in the mixed gas escapes. According to the utility model discloses an embodiment, the refrigerated water entry sets up the upper portion at mist absorption equipment.
The oxidizing solution outlet is for discharging the oxidizing solution from the oxidizing solution absorption tower. The oxidizing solution outlet is connected with the plasma generation and flue gas oxidation equipment. According to an embodiment of the present invention, the oxidizing solution outlet is provided at a lower portion of the mixed gas absorption device.
The air outlet is used for discharging air from the oxidizing solution absorption tower. In certain embodiments, the air outlet is connected to an ion generation and flue gas oxidation apparatus. The oxidizing solution from the oxidizing solution outlet and air from the air outlet are mixed to form an oxidizing atomized liquid. In other embodiments, the air outlet is connected to the ion generating and flue gas oxidation apparatus and the recycled air inlet of the reactor, respectively. Thus, one part of air can be circulated to the reactor, and the other part of air can be conveyed to the ion generation and flue gas oxidation equipment. According to an embodiment of the utility model, the air outlet is connected with the circulating air inlet of ion generation and flue gas oxidation equipment and reactor respectively through the draught fan.
Refrigeration device
The utility model discloses a refrigeration plant can be the refrigerator. The refrigerating device is used for providing chilled water for the mixed gas absorption device. The refrigerating equipment is connected with the chilled water inlet of the mixed gas absorption equipment.
Mother liquor tank
The utility model discloses a mother liquor tank is provided with mother liquor entry and mother liquor export. The reactor 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 the reaction feed liquid is led out to the mother liquid tank; the reactor is provided with a feed liquid inlet; the feed liquid inlet is connected with the mother liquid outlet and is used for circulating the mother liquid in the mother liquid tank to the reactor.
According to the utility model discloses an embodiment, the mother liquor entry links to each other with the feed liquid export of reactor for derive some reaction feed liquid to the mother liquor jar. The mother liquor outlet is connected with the feed liquid inlet of the reactor and is used for circulating the mother liquor in the mother liquor tank to the reactor.
The mother liquor in the mother liquor tank can be directly conveyed back to the reactor, or can be mixed with the raw materials firstly and then conveyed back to the reactor. According to the utility model discloses an embodiment, the mother liquor export is continuous through the mother liquor pump with the feed liquid entry of reactor.
Raw material tank
The utility model discloses can set up a plurality of head tanks. The raw material tank is connected with a corresponding feed inlet of the reactor and is used for supplying raw materials to the reactor. The feedstocks from the different feed tanks may be mixed prior to being supplied to the reactor.
In certain embodiments, the oxidizing solution production apparatus comprises a first raw material tank containing a material a, a second raw material tank containing a material C, a third raw material tank containing a material B, and a fourth raw material tank containing a material S; a plurality of feed inlets are formed in the side wall of the reactor; first head tank, second head tank, third head tank and fourth head tank link to each other with corresponding feed inlet respectively to material A, material C, material B and material S supply to the reactor. In particular, the first raw material tank contains as feed a slurry containing alkali metal chlorate and/or alkali metal chlorite. The second raw material tank contains hydrogen peroxide and/or methanol as a material C. The third raw material tank contains concentrated hydrochloric acid and/or concentrated sulfuric acid as material B. The fourth raw material tank contains urea, sodium humate and/or sodium citrate as the material S. According to an embodiment of the present invention, the oxidizing solution producing apparatus includes a first raw material tank containing a material a, a second raw material tank containing a material C, a third raw material tank containing a material B, and a fourth raw material tank containing a material S. The reactor is provided with a first feed inlet, a second feed inlet, a third feed inlet and a fourth feed inlet. The first feed tank is connected to the first feed port by a first feed pump to feed material a to the reactor. The second feed tank is connected to the second feed port by a second feed pump to feed material C to the reactor. The third raw material tank is connected to the third feed port by a third feed pump, thereby supplying material B to the reactor. The fourth feed tank is connected to the fourth feed port by a fourth feed pump to feed the material S to the reactor.
In other embodiments, the oxidizing solution producing apparatus includes a first raw material tank containing a material a, a second raw material tank containing a material C, a third raw material tank containing a material B, and a fourth raw material tank containing a material S; a first feeding hole, a second feeding hole and a third feeding hole are formed in the side wall of the reactor; the first raw material tank and the second raw material tank are both arranged to be connected with the first feed inlet, so that the material A and the material C are mixed and then are fed to the reactor through the first feed inlet; a third raw material tank is arranged to be capable of being connected with the second feed port so as to feed the material B to the reactor; a fourth feed tank is provided connectable to the third feed port to feed material S to the reactor. In particular, the first raw material tank contains as feed a slurry containing alkali metal chlorate and/or alkali metal chlorite. The second raw material tank contains hydrogen peroxide and/or methanol as a material C. The third raw material tank contains concentrated hydrochloric acid and/or concentrated sulfuric acid as material B. The fourth raw material tank contains urea, sodium humate and/or sodium citrate as the material S. According to an embodiment of the present invention, the oxidizing solution producing apparatus includes a first raw material tank containing a material a, a second raw material tank containing a material C, a third raw material tank containing a material B, and a fourth raw material tank containing a material S. The reactor is provided with a first feed inlet, a second feed inlet and a third feed inlet. The first raw material tank and the second raw material tank are respectively supplied with the material A and the material C through the first feeding pump and the second feeding pump. The material A and the material C are mixed and then are supplied to the reactor through the first feeding hole. The third raw material tank is connected to the second feed port by a third feed pump, thereby supplying material B to the reactor. A fourth feed tank is connected to the third feed port by a fourth feed pump to feed material S to the reactor.
< flue gas denitration apparatus >
The utility model discloses a flue gas denitration device includes oxidizing solution production facility, plasma emergence and flue gas oxidation equipment and denitration equipment. Optionally, the utility model discloses a denitrification facility still includes dust collecting equipment. The utility model discloses a flue gas denitration device is suitable for nitrogen oxide (NOx) concentration more than or equal to 100mg/Nm3. The oxidizing solution production apparatus of the present invention is as described above.
Plasma generation and flue gas oxidation equipment
The utility model discloses a plasma takes place and flue gas oxidation equipment is provided with oxidability atomized liquid entry, and it links to each other with the oxidability solution export of mist absorption equipment and the air outlet of mist absorption equipment respectively. The oxidizing solution from the oxidizing solution outlet is mixed with the air from the air outlet to form atomized liquid, and then the atomized liquid is conveyed to the plasma generation and flue gas oxidation equipment.
The plasma generation and flue gas oxidation equipment is used for converting the oxidizing atomized liquid into liquid oxidizing ions and oxidizing nitrogen oxides in the flue gas to be treated to form oxidized flue gas. For example, the nitrogen oxides (such as NO) in lower valence state in the smoke to be treated are oxidized into nitrogen compounds (such as NO) in higher valence state2). According to one embodiment of the invention, the oxidizing solution is converted into liquid oxidizing ions under the action of the metal or metal compound in the flue gas to be treated, which oxidize the nitrogen oxides in the flue gas to be treated to form oxidized flue gas. Although the principle is not clear, we suspect that the flue gas to be treated from the steel industry contains some metals or metal compounds that promote the conversion of the oxidizing solution into liquid oxidizing ions. The liquid oxidizing ions mean that plasma active substances are present in the liquid. The active material may include oxygen reactive ions, reactive electrons, such as ClO2·、HO·、HO2·、O3And the like.
In certain embodiments, the oxidizing atomization liquid inlet is connected to the oxidizing solution outlet via a transfer pump, and the oxidizing atomization liquid inlet is connected to the air outlet via an induced draft fan.
Denitration equipment
The utility model discloses a denitration device takes place with the plasma and flue gas oxidation equipment links to each other, is used for to coming from plasma takes place and flue gas oxidation equipment's oxidation flue gas carries out denitration treatment in order to obtain the denitration flue gas. The utility model discloses a denitration treatment is preferably semi-dry process or wet process denitration.
The denitration device can comprise an absorption tower, an absorbent bin and a water supply device. The absorption column is preferably a circulating fluidized bed absorption column. The absorption tower is provided with a flue gas inlet and a flue gas outlet. The plasma generation and oxidation equipment is connected with the flue gas inlet and is used for conveying the oxidized flue gas to the absorption tower. The absorbent bin is connected with the absorption tower and is used for supplying the powdery absorbent to the absorption tower. The oxidized flue gas is mixed with an absorbent to form a mixed flue gas. The absorbent may be one or more selected from calcium oxide, calcium hydroxide, magnesium oxide, magnesium hydroxide, sodium carbonate, sodium bicarbonate, fly ash, etc. Preferably, the absorbent is formed by calcium hydroxide and fly ash. The mass ratio of the calcium hydroxide to the fly ash is 1-5: 1, preferably 1.2-4.5: 1, and more preferably 3: 1. The water supply equipment is used for spraying water to the mixed flue gas formed by the absorbent and the oxidized flue gas in the absorption tower.
The flue gas inlet is preferably arranged at the bottom of the absorption column. The absorbent bin is connected with a flue gas pipeline arranged between the flue gas inlet and the venturi section of the absorption tower. The water supply device is connected with the venturi section at the lower part of the absorption tower so as to spray water to the absorption tower to humidify the mixed flue gas formed by the absorbent and the oxidized flue gas. The mixed flue gas continuously rises, and denitration is completed in the absorption tower to obtain the denitration flue gas.
The flue gas outlet is positioned at the top or the upper part of the absorption tower; preferably the top. The dust removal equipment is connected with the flue gas outlet of the absorption tower.
Dust removing equipment
The utility model discloses a dust collecting equipment links to each other with the exhanst gas outlet of absorption tower, is used for coming from exhanst gas outlet's denitration flue gas removes dust and handles in order to obtain clean flue gas and denitration accessory substance.
The dust removing device may comprise a dust remover. The dust removal equipment is connected with the flue gas outlet of the absorption tower. The dedusting equipment is used for dedusting the denitration flue gas to form clean flue gas and denitration byproducts. The dust removing equipment is provided with a clean flue gas outlet and a byproduct outlet. The clean flue gas is discharged from the clean flue gas outlet. According to an embodiment of the utility model, the dust collecting equipment is the sack cleaner.
The dust removing equipment can also comprise a byproduct bin. The byproduct bin is connected with a byproduct outlet of the dust removing equipment and used for receiving denitration byproducts.
The utility model discloses a flue gas denitration device's application method is introduced below, including following step: (1) a step of preparing an oxidizing solution; (2) generating liquid oxidizing ions and oxidizing the flue gas; (3) cigarette with heating meansAnd (4) gas denitration. Optionally, the use method further comprises (4) a step of dust removal. The method has high denitration efficiency, and is suitable for nitrogen oxide (NOx) concentration of 100mg/Nm or more3The flue gas denitration. As described in detail below.
Step of preparing an oxidizing solution
Placing a material R serving as a honeycomb catalyst in a compartment of a reactor, respectively conveying a material A, a material C, a material B and a material S to the reactor by a first raw material tank, a second raw material tank, a third raw material tank and a fourth raw material tank to form a reaction material liquid, and conveying compressed air to the reaction material liquid of the reactor by an air compressor for aeration; generating chlorine dioxide gas as oxidizing gas from the reaction feed liquid; the reactor contains chlorine dioxide gas and air; a blower delivers conditioning air to the vicinity of the mixed gas outlet of the reactor to adjust the concentration of chlorine dioxide in the reactor to form a mixed gas; the frozen water from the refrigerating equipment is sprayed from the upper part of the mixed gas absorption equipment and is mixed with the mixed gas from the reactor in the mixed gas absorption equipment, the chlorine dioxide gas in the mixed gas is solidified in the frozen water to form chlorine dioxide solution as oxidizing solution, and the air in the mixed gas escapes.
The material A of the utility model is slurry containing alkali metal chlorate and/or alkali metal chlorite. Wherein the solute may be selected from one or more of alkali metal chlorate or alkali metal chlorite. Preferably, the concentration of the alkali metal chlorate and/or alkali metal chlorite can be 200-800 g/L, preferably 300-600 g/L, and more preferably 350-500 g/L.
The material B of the utility model can be selected from one or more of concentrated hydrochloric acid or concentrated sulfuric acid. Preferably, the material B is concentrated sulfuric acid. The concentration of the concentrated sulfuric acid may be 80 to 99.9 wt%, preferably 85 to 98 wt%.
The material C of the utility model can be selected from one or more of hydrogen peroxide and methanol. Preferably, the material C is hydrogen peroxide.
The material S of the utility model is a stabilizing agent and can be selected from one or more of urea, sodium humate and sodium citrate. Preferably, the material S is selected from one of urea or sodium humate.
Preferably, the material R may be a transition metal oxide. The material R may be selected from one or more of iron oxide, manganese oxide or cerium oxide. Preferably, R is ferric oxide.
The utility model discloses in, the quantity of alkali metal chlorate and/or alkali metal chlorite in material A is 1 ~ 10 parts by weight, and material B 'S quantity is 1 ~ 5 parts by weight, and material C' S quantity is 1 ~ 5 parts by weight, and material R 'S quantity is 0.002 ~ 0.02 parts by weight, and material S' S quantity is 0.01 ~ 0.3 parts by weight. Preferably, the amount of the alkali metal chlorate and/or alkali metal chlorite in the material A is 1-6 parts by weight, the amount of the material B is 1-3 parts by weight, the amount of the material C is 1-4 parts by weight, the amount of the material R is 0.002-0.01 part by weight, and the amount of the material S is 0.01-0.2 part by weight.
According to one embodiment of the present invention, material a is sodium chlorate, material B is concentrated sulfuric acid, material C is hydrogen peroxide, R is ferric oxide, and material S is urea or sodium humate. According to a specific embodiment of the present invention, material a is sodium chlorate, material B is concentrated sulfuric acid, material C is hydrogen peroxide, R is ferric oxide, and material S is sodium humate.
The reaction time of the material A, the material B, the material C, the material S and the material R can be 2-8 hours; preferably 3-6 h; more preferably 4-5 h. The reaction temperature can be 45-85 ℃; preferably 50-75 ℃; more preferably 55 to 60 ℃. And conveying steam for heating to the reactor through a steam inlet, and heating the raw materials in a heat exchange mode.
In certain embodiments, feed a, feed B are added to the reactor. When the acidity of the reaction feed liquid in the reactor reaches 4-9N, preferably 5-8N, more preferably 6-7N, and the concentration of A reaches 200-800 g/L, preferably 300-600 g/L, more preferably 400-600 g/L, the material C and the material S are conveyed into the reactor. This is advantageous in that the reaction proceeds smoothly.
The utility model discloses a have a plurality of compartments in the reactor, material R as honeycomb catalyst sets up in at least some compartments. The reaction liquid in the previous compartment overflows to the next compartment, thereby completing the multi-stage reaction. The material R is preferably arranged in all compartments.
In some embodiments, the reaction feed liquid of the reactor is led out to a mother liquid tank, and the mother liquid in the mother liquid tank is recycled to the reactor. For example, the mother liquor in the mother liquor tank is mixed with the feed B from the third feed tank and recycled to the reactor. Thus, the reaction progress can be controlled, and the over-high concentration of chlorine dioxide in the reactor can be avoided.
The concentration of chlorine dioxide in the mixed gas can be 1-10 vol%; preferably 2-8 vol%; more preferably 2 to 6 vol%. This improves the operational safety.
The temperature of the chilled water can be 2-15 ℃; preferably 3-10 ℃; more preferably 5 to 10 ℃. This allows chlorine dioxide to be stably present in the solution.
The concentration of chlorine dioxide in the chlorine dioxide solution can be 1-25 wt%; preferably 1 to 20 wt%; more preferably 7 to 15 wt%. Thus, the oxidation effect can be ensured, and the operation safety can be improved.
Generating gaseous oxidizing ions and oxidizing the flue gas
And mixing the chlorine dioxide solution from the mixed gas absorption equipment with air from the mixed gas absorption equipment to form an oxidizing atomized liquid, and then conveying the oxidizing atomized liquid to plasma generation and flue gas oxidation equipment. In the plasma generation and flue gas oxidation equipment, oxidizing atomized liquid is converted into liquid oxidizing ions under the action of metal or metal compounds in flue gas to be treated, and the liquid oxidizing ions oxidize nitric oxides in the flue gas to be treated to form oxidized flue gas. The metal or metal compound is the residual impurity in the smoke to be treated. The present invention unexpectedly utilizes these impurities to convert the oxidizing gas into gaseous oxidizing ions, thereby promoting the oxidation reaction of the nitrogen oxides. The flue gas to be treated in the utility model is preferably flue gas from the steel industry; such as flue gases from steel pelletizing processes or steel sintering processes.
In the present invention, a part of the air from the air outlet may also be circulated into the reactor. In certain embodiments, air may be circulated to the reactor by an induced draft fan. The induced draft fan makes negative pressure form in the reactor. The pressure in the reactor can be-1.0 to-5 kPa; preferably-1.2 to-3.5 kPa; more preferably-1.5 to-3.0 kPa.
The temperature of the flue gas in the flue gas to be treated can be 80-200 ℃; preferably 80-150 ℃; more preferably 100 to 130 ℃. The content of the sulfur dioxide can be 700-2000 mg/Nm3(ii) a Preferably 1000 to 1800mg/Nm3(ii) a More preferably 1000 to 1500mg/Nm3. The content of nitrogen oxides can be 100-500 mg/Nm3(ii) a Preferably 100 to 400mg/Nm3(ii) a More preferably 100 to 300mg/Nm3
The time for the oxidizing gas to contact with the flue gas to be treated in the plasma generation and flue gas oxidation equipment can be 0.3-5 s; preferably 1 to 3 s; more preferably 1 to 2 seconds. This is beneficial to compromise the nitrogen oxide oxidation rate and the treatment efficiency.
Denitration step of flue gas
And (4) denitrating the oxidized flue gas in denitration equipment. Conveying the oxidized flue gas to an absorption tower, conveying the absorbent from a powdery absorbent bin to a flue gas pipeline arranged between a flue gas inlet and a venturi section of the absorption tower, and mixing the oxidized flue gas and the absorbent to form mixed flue gas. And water is sprayed to the venturi section at the lower part of the absorption tower through a water supply device, so that the mixed flue gas is humidified. The mixed flue gas continuously rises, and denitration is completed in the absorption tower to obtain the denitration flue gas.
The absorbent may be one or more selected from calcium oxide, calcium hydroxide, magnesium oxide, magnesium hydroxide, sodium carbonate, sodium bicarbonate, fly ash, etc. Preferably, the absorbent is formed by calcium hydroxide and fly ash. The mass ratio of the calcium hydroxide to the fly ash is 1-5: 1, preferably 1.2-4.5: 1, and more preferably 3: 1.
Dust removal step
And conveying the denitration flue gas from the absorption tower to dust removal equipment to form clean flue gas and denitration byproducts. And discharging the clean flue gas from the chimney. And conveying one part of denitration byproducts to a byproduct bin, and conveying the other part of denitration byproducts to an absorption tower for recycling.
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%. Sodium chlorate slurry: the sodium chlorate solid is dispersed in water to form the sodium chlorate solid with the concentration of 500 g/L.
Example 1
Fig. 1 is a schematic view of an oxidizing solution production apparatus according to the present invention. The oxidizing solution production apparatus of the present embodiment includes a first raw material tank 1, a second raw material tank 2, a third raw material tank 3, a fourth raw material tank 4, a reactor 10, an air blower 12, an air compressor 13, a mother liquor tank 14, a mixed gas absorption apparatus 16, and a refrigeration apparatus 17.
The side wall of the reactor 10 is provided with a plurality of feed inlets, including a first feed inlet, a second feed inlet, a third feed inlet and a fourth feed inlet. The first and second raw material tanks 1 and 2 are connected to the first and second feed ports by first and second feed pumps 6 and 7, respectively, to feed a material a (e.g., an alkali metal chlorate-containing slurry or an alkali metal chlorite-containing slurry) and a material C (e.g., hydrogen peroxide or methanol) to the reactor 10, respectively. The third raw material tank 3 and the fourth raw material tank 4 are respectively connected with a third feed port and a fourth feed port through a third feed pump 8 and a fourth feed pump 9, so as to respectively supply a material B (such as concentrated hydrochloric acid or concentrated sulfuric acid) and a material S (such as a stabilizer selected from urea, sodium humate or sodium citrate) to the reactor 10. This forms the reaction feed.
The reactor 10 is provided with a compressed air inlet (not shown) at an upper portion of a sidewall thereof. An air compressor 13 is connected to the compressed air inlet for supplying compressed air to the reaction feed liquid in the reactor 10. Compressed air is aerated in the reactor 10 to sufficiently stir the reaction feed liquid to generate an oxidizing gas, such as chlorine dioxide gas.
The top of the reactor 10 is also provided with an air inlet for conditioning (not shown). A blower 12 is connected to the conditioning air inlet to blow air into the vicinity of the mixed gas outlet of the reactor 10, thereby adjusting the concentration of chlorine dioxide in the reactor 10 to obtain a mixed gas.
The upper part of the reactor 10 is provided with a feed liquid outlet for leading out the reaction feed liquid to a mother liquid tank 14. The mother liquor tank 14 is provided with a mother liquor inlet and a mother liquor outlet. The mother liquid inlet is connected with the feed liquid outlet. The mother liquor outlet is connected to the reactor 10 by a mother liquor pump 15. The material B from the third raw material tank 3 is mixed with the mother liquor and then circulated to the reactor 10.
The mixed gas absorption apparatus 16 is an absorption tower. The top of the reactor 10 is provided with a mixed gas outlet (not shown). A mixed gas absorption device 16 is connected to the mixed gas outlet for converting the oxidizing gas in the mixed gas into a solution, forming an oxidizing solution and air. The upper part of the mixed gas absorption device 16 is also provided with an air outlet (not shown) connected to the reactor 10 by an induced draft fan 19 for circulating at least a part of the air to the reactor 10.
The refrigeration equipment 17 of the present embodiment is a freezer. The upper portion of the mixed gas absorption device 16 is provided with a chilled water inlet (not shown). The refrigerating device 17 is connected to the chilled water inlet for supplying chilled water 18 to the mixed gas absorbing device 16. After the chilled water 18 from the refrigerating device 17 is sprayed downward from above the mixed gas absorbing device 16 and mixed with the mixed gas entering from below, the oxidizing gas is fixed in the chilled water to form an oxidizing solution (for example, a chlorine dioxide solution), and the air in the mixed gas escapes.
Example 2
The same as in example 1 except for the following settings:
as shown in fig. 2, a first feed port, a second feed port, and a third feed port (not shown) are provided on the side wall of the reactor 10. The first material tank 1 and the second material tank 2 are respectively supplied with a material a and a material C by a first supply pump 6 and a second supply pump 7. The material A and the material C are mixed and then supplied to the reactor 10 through the first feed port. The third raw material tank 3 is connected to the second feed port by a third feed pump 8 to feed the material B to the reactor 10. The fourth raw material tank 4 is connected to the third feed port by a fourth feed pump 9 to feed the material S to the reactor 10. This forms the reaction feed.
Example 3
Fig. 3 is the utility model discloses a flue gas denitration device's schematic diagram. The flue gas denitration device of the embodiment comprises oxidizing solution production equipment, plasma generation and flue gas oxidation equipment 21, denitration equipment and dust removal equipment. The oxidizing solution production apparatus includes a first raw material tank 1, a second raw material tank 2, a third raw material tank 3, a fourth raw material tank 4, a reactor 10, a blower 12, an air compressor 13, a mother liquor tank 14, a mixed gas absorption apparatus 16, and a refrigeration apparatus 17. The denitration device comprises an absorbent bin 22, a water supply device 23 and a denitration absorption tower 24. The dust removing apparatus includes a dust remover 25, a byproduct bin 26, and a stack 27.
The side wall of the reactor 10 is provided with a plurality of feed inlets, including a first feed inlet, a second feed inlet, a third feed inlet and a fourth feed inlet. The first and second raw material tanks 1 and 2 are connected to the first and second feed ports by first and second feed pumps 6 and 7, respectively, to feed a material a (e.g., an alkali metal chlorate-containing slurry or an alkali metal chlorite-containing slurry) and a material C (e.g., hydrogen peroxide or methanol) to the reactor 10, respectively. The third raw material tank 3 and the fourth raw material tank 4 are respectively connected with a third feed port and a fourth feed port through a third feed pump 8 and a fourth feed pump 9, so as to respectively supply a material B (such as concentrated hydrochloric acid or concentrated sulfuric acid) and a material S (such as a stabilizer selected from urea, sodium humate or sodium citrate) to the reactor 10. This forms the reaction feed.
The reactor 10 is provided with a compressed air inlet (not shown) at an upper portion of a sidewall thereof. An air compressor 13 is connected to the compressed air inlet for supplying compressed air to the reaction feed liquid in the reactor 10. Compressed air is aerated in the reactor 10 to sufficiently stir the reaction feed liquid to generate an oxidizing gas, such as chlorine dioxide gas.
The top of the reactor 10 is also provided with an air inlet for conditioning (not shown). A blower 12 is connected to the conditioning air inlet to blow air into the vicinity of the mixed gas outlet of the reactor 10, thereby adjusting the concentration of chlorine dioxide in the reactor 10 to obtain a mixed gas.
The upper part of the reactor 10 is provided with a feed liquid outlet for leading out the reaction feed liquid to a mother liquid tank 14. The mother liquor tank 14 is provided with a mother liquor inlet and a mother liquor outlet. The mother liquid inlet is connected with the feed liquid outlet. The mother liquor outlet is connected to the reactor 10 by a mother liquor pump 15. The material B from the third raw material tank 3 is mixed with the mother liquor and then circulated to the reactor 10.
The mixed gas absorption apparatus 16 is an absorption tower. The top of the reactor 10 is provided with a mixed gas outlet (not shown). A mixed gas absorption device 16 is connected to the mixed gas outlet for converting the oxidizing gas in the mixed gas into a solution, forming an oxidizing solution and air.
The refrigeration equipment 17 of the present embodiment is a freezer. The upper portion of the mixed gas absorption device 16 is provided with a chilled water inlet (not shown). The refrigerating device 17 is connected to the chilled water inlet for supplying chilled water 18 to the mixed gas absorbing device 16. After the chilled water 18 from the refrigerating device 17 is sprayed downward from above the mixed gas absorbing device 16 and mixed with the mixed gas entering from below, the oxidizing gas is fixed in the chilled water to form an oxidizing solution (for example, a chlorine dioxide solution), and the air in the mixed gas escapes.
The mixed gas absorbing device 16 is further provided at a lower portion thereof with an oxidizing solution outlet (not shown) connected to a plasma generating and flue gas oxidizing device 21 via a transfer pump 20. The upper part of the mixed gas absorption device 16 is provided with an air outlet which is respectively connected with the reactor 10 and the plasma generation and flue gas oxidation device 21 through a draught fan 19. A portion of the air in the mixed gas absorption device 16 is fed back to the reactor 10, and another portion of the air is mixed with the oxidizing solution discharged from the oxidizing solution outlet to form an oxidizing atomized liquid, which is sprayed to the plasma generation and flue gas oxidation device 21.
In the plasma generation and flue gas oxidation apparatus 21, the oxidizing atomized liquid is converted into liquid oxidizing ions under the action of metal or metal compounds in the flue gas to be treated (for example, sintering flue gas or pelletizing flue gas in the steel industry), and the nitrogen oxides in low valence state in the flue gas to be treated are oxidized into nitrogen-containing compounds in high valence state, so as to obtain oxidized flue gas.
The denitration absorption tower 24 is a circulating fluidized bed absorption tower. The denitration absorption tower 24 has a flue gas inlet (not shown) at the bottom. The plasma generation and flue gas oxidation device 21 is connected to the flue gas inlet to deliver the oxidized flue gas to the absorber tower 24. The absorbent bin 22 is connected to a flue gas duct provided between the flue gas inlet and the venturi section of the denitration absorption tower 24 to supply the powdery absorbent thereto. The oxidized flue gas is mixed with an absorbent in the flue gas duct to form a mixed flue gas. The water supply device 22 is connected to a venturi section located at a lower portion of the denitration absorption tower 24 so as to spray water to the denitration absorption tower 24 to humidify the mixed flue gas. The mixed flue gas continuously rises, and denitration is completed in the denitration absorption tower 24 to obtain the denitration flue gas.
The denitration absorption tower 24 has a flue gas outlet (not shown) at the top or upper portion thereof. The dust removing device 25 is a bag-type dust remover and is connected with the flue gas outlet of the denitration absorption tower 24. The upper part of the dust-removing device 25 is connected to a chimney 27. The lower portion of the dust removing device 25 is connected to a by-product bin 26. The denitration flue gas is discharged from the flue gas outlet and enters the dust removal equipment 25. The dedusting equipment 25 carries out dedusting treatment on the denitration flue gas. The resulting clean flue gas is discharged from the stack 27; the obtained denitration by-product is conveyed to the by-product bin 26.
Example 4
The same as example 3 except for the following settings:
as shown in fig. 4, a first feed port, a second feed port, and a third feed port (not shown) are provided on the side wall of the reactor 10. The first material tank 1 and the second material tank 2 are respectively supplied with a material a and a material C by a first supply pump 6 and a second supply pump 7. The material A and the material C are mixed and then supplied to the reactor 10 through the first feed port. The third raw material tank 3 is connected to the second feed port by a third feed pump 8 to feed the material B to the reactor 10. The fourth raw material tank 4 is connected to the third feed port by a fourth feed pump 9 to feed the material S to the reactor 10. This forms the reaction feed.
Example 5
The denitration device of embodiment 4 is adopted for denitration of flue gas, and the method comprises the following specific steps:
sodium chlorate slurry (material a) from the first feed tank 1, hydrogen peroxide (material C) from the second feed tank 2, concentrated sulfuric acid (material B) from the third feed tank 3 and urea (material S) from the fourth feed tank 4 are fed to the reactor 10 to form a reaction feed.
The reaction feed liquid reacts under a honeycomb catalyst 5 (honeycomb ferric oxide R) arranged in the compartment. The reaction liquid in the previous compartment overflows to the next compartment through the baffling pipe, thereby completing the multi-stage reaction. Steam for heating is conveyed to the reactor 10 through a steam inlet 11, and the raw materials are heated in a heat exchange mode. The compressed air from the air compressor 13 is supplied to the reaction liquid in the reactor 10 to aerate the reaction liquid, and chlorine dioxide gas is generated by the reaction. Reactor 10 contains chlorine dioxide gas and air. The conditioning air was sent to the vicinity of the mixed gas outlet of the reactor 10 by the blower 12 to adjust the concentration of chlorine dioxide in the reactor 10 to 2 vol% to obtain a mixed gas. The feed liquid from the reactor 10 is led out to a mother liquid tank 14, and the mother liquid in the mother liquid tank 14 is mixed with concentrated sulfuric acid (B) from a third raw material tank by a mother liquid pump 15 and then sent back to the reactor 10.
Chlorine dioxide gas from reactor 10 is delivered to mixed gas absorption unit 16. The chilled water 18 from the freezer 17 is sprayed downward from the upper part of the mixed gas absorption device 16 and then mixed with the mixed gas entering from the lower part of the mixed gas absorption device 16, chlorine dioxide is fixed in the chilled water to obtain a chlorine dioxide solution with a concentration of 10 wt%, and air in the mixed gas escapes.
Air is led out from an air outlet of the mixed gas absorption device 16 through an induced draft fan 19; a portion of the air is fed back into the reactor 10 and another portion of the air is mixed with the oxidizing solution from the mixed gas outlet of the mixed gas absorption device 16 to form an oxidizing atomized liquid. The oxidizing atomized liquid is sprayed to the plasma generation and flue gas oxidation equipment 21.
In the plasma generation and flue gas oxidation apparatus 21, the oxidizing atomized liquid is converted into liquid oxidizing ions under the action of metal or metal compound in the flue gas to be treated, and the nitrogen oxide in low valence state in the flue gas to be treated is oxidized into nitrogen-containing compound in high valence state, thereby obtaining oxidized flue gas.
The oxidized flue gas is conveyed to the denitration absorption tower 24. Powdered absorbent (formed from calcium hydroxide and fly ash) from the absorbent bin 22 is conveyed into the flue gas duct disposed between the flue gas inlet and the venturi section of the denitration absorber 24, and the oxidized flue gas is mixed with the absorbent to form mixed flue gas. Water is sprayed to a venturi section located at the lower portion of the denitration absorption tower 24 through the water supply device 23, so that the mixed flue gas is humidified. The mixed flue gas continuously rises, and denitration is completed in the denitration absorption tower 24 to obtain the denitration flue gas.
The denitrated flue gas from the denitrated absorption tower 24 is conveyed to a dust removal device 25, forming clean flue gas and denitrated byproducts. Clean flue gas is discharged from the stack 27. A part of the denitration by-products is conveyed to the by-product bin 26, and the other part of the denitration by-products is conveyed to the denitration absorption tower 24 for recycling.
The raw materials and the dosage thereof are shown in Table 1, and the yield of the chlorine dioxide is 3.5 t/d.
The flue gas to be treated comes from 230m2Specific parameters of the sintering machine items are shown in table 2.
The time for contacting the oxidizing atomized liquid and the flue gas to be treated in the plasma generation and flue gas oxidation device 21 is 2.2 s. By analyzing the components of different nitrogen oxides in the oxidized smoke, the oxidation rate of NO is 90 percent, and the NO is mainly oxidized into NO2And HNO3，HNO3In the form of nitric acid vapour.
The clean smoke parameters are shown in table 3. The operation is carried out for 8 months, and the operation safety is high.
TABLE 1
| Raw materials | Dosage (parts by weight) |
| Sodium chlorate in sodium chlorate slurry (A) | 4.5 |
| Concentrated sulfuric acid (B) | 3 |
| Hydrogen peroxide (C) | 3.2 |
| Iron oxide (R) | 0.007 |
| Urea (S) | 0.15 |
TABLE 2
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 1380000 |
| Standard flue gas volume | Nm3/h | 940000 |
| Concentration of NOx | mg/Nm3 | 250 |
| Dust content | mg/Nm3 | 110 |
| Temperature of | ℃ | 130 |
| Moisture content | ％ | 15.6 |
TABLE 3
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 1590000 |
| Standard flue gas volume | Nm3/h | 1170000 |
| Concentration of NOx | mg/Nm3 | 30 |
| Dust | mg/Nm3 | 1.5 |
| Temperature of | ℃ | 97 |
| Denitration efficiency | ％ | 88 |
Example 6
Example 5 was followed, except for the following parameters:
the raw materials and the amounts thereof were as shown in Table 4, and the yield of chlorine dioxide was 1.3 t/d.
The flue gas to be treated comes from 144m2Specific parameters of the sintering machine items are shown in table 5.
The time for contacting the oxidizing atomized liquid and the flue gas to be treated in the plasma generation and flue gas oxidation device 21 is 1.5 s. By analyzing the components of different nitrogen oxides in the oxidized smoke, the oxidation rate of NO is 90.5 percent, and the NO is mainly oxidized into NO2And HNO3，HNO3In the form of nitric acid vapour.
The clean smoke parameters are shown in table 6. The operation is carried out for 8 months, and the operation safety is high.
TABLE 4
| Raw materials | Dosage (parts by weight) |
| Sodium chlorate in sodium chlorate slurry (A) | 2 |
| Concentrated sulfuric acid (B) | 1.7 |
| Hydrogen peroxide (C) | 1.8 |
| Iron oxide (R) | 0.004 |
| Humic acid sodium salt (S) | 0.03 |
TABLE 5
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 860000 |
| Standard flue gas volume | Nm3/h | 590000 |
| Concentration of NOx | mg/Nm3 | 180 |
| Dust content | mg/Nm3 | 110 |
| Temperature of | ℃ | 130 |
| Moisture content | ％ | 15.6 |
TABLE 6
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 910000 |
| Standard flue gas volume | Nm3/h | 630000 |
| Concentration of NOx | mg/Nm3 | 25 |
| Dust | mg/ |
1 |
| Temperature of | ℃ | 97 |
| Denitration efficiency | ％ | 86 |
Example 7
Example 5 was followed, except for the following parameters:
the raw materials and the amounts thereof were as shown in Table 7, and the yield of chlorine dioxide was 2.5 t/d.
The flue gas to be treated comes from 180m2In the sintering machine project, specific parameters are asShown in Table 8.
The time for contacting the oxidizing atomized liquid and the flue gas to be treated in the plasma generation and flue gas oxidation device 21 is 2 s. By analyzing the components of different nitrogen oxides in the oxidized smoke, the oxidation rate of NO is 91 percent, and the NO is mainly oxidized into NO2And HNO3，HNO3In the form of nitric acid vapour.
The clean smoke parameters are shown in table 9. The operation is carried out for 8 months, and the operation safety is high.
TABLE 7
| Raw materials | Dosage (parts by weight) |
| Sodium chlorate in sodium chlorate slurry (A) | 3.8 |
| Concentrated sulfuric acid (B) | 2.6 |
| Hydrogen peroxide (C) | 2.8 |
| Iron oxide (R) | 0.007 |
| Humic acid sodium salt (S) | 0.07 |
TABLE 8
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 1080000 |
| Standard flue gas volume | Nm3/h | 740000 |
| Concentration of NOx | mg/Nm3 | 240 |
| Dust content | mg/Nm3 | 110 |
| Temperature of | ℃ | 125 |
| Moisture content | ％ | 15.6 |
TABLE 9
| Parameter(s) | Unit of | Numerical value |
| Flue gas volume (working condition) | m3/h | 1120000 |
| Standard flue gas volume | Nm3/h | 880000 |
| Concentration of NOx | mg/Nm3 | 28 |
| Dust | mg/ |
1 |
| Temperature of | ℃ | 95 |
| Denitration efficiency | ％ | 88 |
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 oxidizing solution producing apparatus, comprising:
a reactor for preparing an oxidizing gas from the reaction feed liquid and forming a mixed gas with air; it is provided with a compressed air inlet, an air inlet for regulation and a mixed gas outlet;
an air compressor disposed in connection with the compressed air inlet for providing compressed air to the reactor;
a blower connected to the conditioning air inlet for supplying conditioning air to the reactor;
the mixed gas absorption device is arranged to be connected with the mixed gas outlet and is used for converting oxidizing gas in the mixed gas into a solution to form oxidizing solution and air;
and the refrigerating device is arranged to be connected with the mixed gas absorption device and is used for providing the chilled water for the mixed gas absorption device.
2. The oxidizing solution producing apparatus according to claim 1, wherein said reactor is further provided with a circulating air inlet, and said mixed gas absorbing apparatus further has an air outlet connected to the circulating air inlet for circulating at least a portion of the air to the reactor.
3. The oxidizing solution producing apparatus according to claim 1, wherein said reactor is further provided with a steam inlet for supplying steam for heating to said reactor.
4. The oxidizing solution production apparatus according to claim 1, wherein said reactor is a horizontal, parallel flow reactor; at least one partition is arranged in the reactor and can divide the inner space of the reactor into a plurality of compartments; in at least a part of the compartments, a honeycomb catalyst is provided for catalyzing the reaction feed to obtain oxidizing gases.
5. The oxidizing solution producing apparatus according to claim 4, wherein a baffle pipe is provided between said compartments, and said baffle pipe is used for overflowing the reaction feed liquid of a preceding compartment to a next compartment.
6. An oxidizing solution production apparatus according to claim 1, characterized in that:
the oxidizing solution production equipment also comprises a mother liquor tank, wherein the mother liquor tank is provided with a mother liquor inlet and a mother liquor outlet;
the reactor 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 reactor is provided with a feed liquid inlet; the feed liquid inlet is connected with the mother liquid outlet and is configured to circulate the mother liquid in the mother liquid tank to the reactor.
7. An oxidizing solution production apparatus according to claim 1, characterized in that:
the oxidizing solution production equipment further comprises a first raw material tank containing a material A, a second raw material tank containing a material C, a third raw material tank containing a material B and a fourth raw material tank containing a material S;
a first feed port, a second feed port, a third feed port and a fourth feed port are arranged on the side wall of the reactor; first head tank is connected with first feed inlet to supply with material A to the reactor, the second head tank is connected with the second feed inlet, thereby supply with material C to the reactor, the third head tank links to each other with the third feed inlet, thereby supply with material B to the reactor, the fourth head tank leads to and links to each other with the fourth feed inlet, thereby supplies with material S to the reactor, forms the reaction feed liquid.
8. An oxidizing solution production apparatus according to claim 1, characterized in that:
the oxidizing solution production equipment further comprises a first raw material tank containing a material A, a second raw material tank containing a material C, a third raw material tank containing a material B and a fourth raw material tank containing a material S;
a first feeding hole, a second feeding hole and a third feeding hole are formed in the side wall of the reactor;
the first raw material tank and the second raw material tank are both arranged to be connected with the first feed inlet, so that the material A and the material C are mixed and then are fed to the reactor through the first feed inlet;
a third raw material tank is arranged to be capable of being connected with the second feed port so as to feed the material B to the reactor;
a fourth feed tank is provided connectable to the third feed port to supply material S to the reactor to form a reaction feed.
9. The oxidizing solution producing apparatus according to claim 7 or 8, characterized in that:
a first feed tank containing as feed a slurry comprising alkali metal chlorate and/or alkali metal chlorite;
the second raw material tank contains hydrogen peroxide and/or methanol as a material C;
the third raw material tank contains concentrated hydrochloric acid and/or concentrated sulfuric acid serving as a material B;
the fourth raw material tank contains urea, sodium humate and/or sodium citrate as the material S.
10. A flue gas denitration device, which is characterized by comprising:
the oxidizing solution producing apparatus according to claim 1, said mixed gas absorbing apparatus further having an oxidizing solution outlet and an air outlet;
the plasma generation and flue gas oxidation equipment is provided with an oxidizing atomized liquid inlet, and the oxidizing solution outlet and the air outlet are respectively connected with the oxidizing atomized liquid inlet, so that oxidizing solution and air are mixed to form oxidizing atomized liquid and then enter the plasma generation and flue gas oxidation equipment; the plasma generation and flue gas oxidation equipment is arranged to convert the oxidizing atomized liquid into liquid oxidizing ions and oxidize nitric oxides in the flue gas to be treated to form oxidized flue gas;
and the denitration device is connected with the plasma generation and flue gas oxidation device and is arranged to be capable of carrying out denitration treatment on the oxidized flue gas from the plasma generation and flue gas oxidation device so as to obtain the denitration flue gas.
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| CN111167299A (en) * | 2020-03-02 | 2020-05-19 | 中晶蓝实业集团有限公司 | Flue gas denitration device based on liquid oxidizing ions and application method thereof |
| CN113413759A (en) * | 2021-07-08 | 2021-09-21 | 南京中电环保科技有限公司 | Treatment system for absorbing nitrogen oxides by forced oxidation-reduction |
| 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 |
| CN115105948A (en) * | 2022-05-23 | 2022-09-27 | 中国环境科学研究院 | Process for removing nitrogen oxides in low-temperature waste gas |
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| CN111167299A (en) * | 2020-03-02 | 2020-05-19 | 中晶蓝实业集团有限公司 | Flue gas denitration device based on liquid oxidizing ions and application method thereof |
| CN111167299B (en) * | 2020-03-02 | 2024-02-27 | 中晶环境科技股份有限公司 | Flue gas denitration device based on liquid oxidizing ions and application method thereof |
| 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 |
| CN113413759A (en) * | 2021-07-08 | 2021-09-21 | 南京中电环保科技有限公司 | Treatment system for absorbing nitrogen oxides by forced oxidation-reduction |
| CN115105948A (en) * | 2022-05-23 | 2022-09-27 | 中国环境科学研究院 | Process for removing nitrogen oxides in low-temperature waste gas |
| CN115105948B (en) * | 2022-05-23 | 2023-09-26 | 中国环境科学研究院 | Process for removing nitrogen oxides in low-temperature waste gas |
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Effective date of registration: 20201210 Address after: 100176 Ronghua International Building No. 3, 10 Ronghua South Road, Beijing Daxing Economic and Technological Development Zone, 20th Floor Patentee after: Shanghui TONG Address before: 100176 Ronghua International Building No. 3, 10 Ronghua South Road, Beijing Daxing Economic and Technological Development Zone, 20th Floor Patentee before: Zhongjing Kunlun Industrial Group Co., Ltd |