CN110694470A - System and method for flue gas desulfurization and denitration by using methane - Google Patents

System and method for flue gas desulfurization and denitration by using methane Download PDF

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CN110694470A
CN110694470A CN201911052117.3A CN201911052117A CN110694470A CN 110694470 A CN110694470 A CN 110694470A CN 201911052117 A CN201911052117 A CN 201911052117A CN 110694470 A CN110694470 A CN 110694470A
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methane
flue gas
desulfurization
reaction device
denitration
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刘蓉
王晓龙
郜时旺
王琪
肖天存
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Huaneng Clean Energy Research Institute
China Huaneng Group Co Ltd
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China Huaneng Group Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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    • B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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Abstract

The invention discloses a system and a method for flue gas desulfurization and denitration by using methane, and belongs to the technical field of desulfurization and denitration. Comprises a methane lean-oxygen combustion reaction device, a flue gas desulfurization and denitrification reaction device, a catalyst regenerator, a cyclone separator, a cooling tower and a heat exchanger. Firstly, deoxidizing the flue gas in a methane lean oxygen combustion reaction device, then reacting sulfur oxides and methane in the flue gas in a fluidized bed reactor in the presence of a catalyst to generate elemental sulfur, generating nitrogen from nitrogen oxides, and converting methane into carbon dioxide and water vapor. The system has reasonable structural design, wide sources of methane as a reducing agent, low cost and convenient storage and use; the desulfurization and denitrification are carried out simultaneously, the pollutant treatment efficiency is improved, the recycling of sulfur element can be realized, waste is changed into valuable, other waste residues and waste liquid are not generated, no secondary pollution is caused, the environment friendliness is realized, and economic benefits are brought.

Description

System and method for flue gas desulfurization and denitration by using methane
Technical Field
The invention belongs to the technical field of desulfurization and denitrification, and particularly relates to a system and a method for performing flue gas desulfurization and denitrification by using methane.
Background
The main source of acid rain formation is the large amount of sulfur dioxide pollutants discharged during the process of energy consumption mainly by coal burning. The total amount of the sulfur oxides and the nitrogen oxides discharged by thermal power plants which pollute a large number of households is mainly reduced by controlling the total amount of the sulfur oxides and the nitrogen oxides discharged by the thermal power plants to treat the acid rain pollution.
Low concentration of SO2(the concentration is lower than 3%) if the traditional oxidation method and desulfurization acid preparation are adopted, the technical and economic difficulty is great, a large amount of water is consumed in wet desulfurization, the adsorption method requires frequent regeneration and subsequent treatment of the catalyst, the secondary pollution problem exists, and the sulfur element is wasted and cannot be recovered. Most of the current researches are the technologies of simultaneous desulfurization and denitrification by an ammonia process, and the technologies of simultaneous desulfurization and denitrification by an ammonia process also have self defects, mainly include large furnace size, large boiler pressure change, easy ammonia leakage and easy secondary pollution.
Disclosure of Invention
In order to solve the existing problems, the invention aims to provide a system and a method for performing flue gas desulfurization and denitration by using methane, which realize the recycling of sulfur element while performing desulfurization and denitration, do not generate other waste residues and liquid, have no secondary pollution, and have low cost and high economic benefit.
The invention is realized by the following technical scheme:
the invention discloses a system for performing flue gas desulfurization and denitration by using methane, which comprises a methane lean-oxygen combustion reaction device, a flue gas desulfurization and denitration reaction device, a catalyst regenerator, a cyclone separator, a cooling tower and a heat exchanger, wherein the methane lean-oxygen combustion reaction device is connected with the cooling tower;
an inlet of the methane lean-oxygen combustion reaction device is connected with a flue gas pipeline to be treated and a first branch of methane raw gas, an outlet of the methane lean-oxygen combustion reaction device is connected with an inlet of the flue gas desulfurization and denitrification reaction device, an inlet of the flue gas desulfurization and denitrification reaction device is also connected with a second branch of methane raw gas, and a solid outlet of the flue gas desulfurization and denitrification reaction device is connected with a solid inlet of a catalyst regenerator; a gas outlet of the flue gas desulfurization and denitration reaction device is connected with an inlet of a cyclone separator, an outlet of a catalyst regenerator is connected with an inlet of the flue gas desulfurization and denitration reaction device, a solid outlet of the cyclone separator is connected with a solid inlet of the catalyst regenerator, and a gas inlet of the catalyst regenerator is connected with a third branch of methane feed gas; the gas outlet of the cyclone separator is connected with the inlet of the cooling tower, the gas outlet of the cooling tower is connected with the heat exchanger, the heat exchanger is connected with a methane raw gas pipeline, and the methane raw gas pipeline is connected with a methane raw gas first branch, a methane raw gas second branch and a methane raw gas third branch.
Preferably, a plug valve is arranged on a connecting pipeline between a solid outlet of the flue gas desulfurization and denitrification reaction device and a solid inlet of the catalyst regenerator.
Preferably, the catalysts in the methane lean-oxygen combustion reaction device and the flue gas desulfurization and denitrification reaction device are supported metal oxide catalysts.
Further preferably, the catalyst of the supported metal oxide catalyst is one or more of simple substances of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium, and the carrier is one or more of oxides of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium.
Preferably, the methane lean oxygen combustion reaction device is a fixed bed reactor.
Preferably, the flue gas desulfurization and denitrification reaction device is a fluidized bed reactor.
The invention discloses a method for performing flue gas desulfurization and denitration by using methane, which comprises the following steps:
the methane raw material gas in the methane raw material gas pipeline is divided into a first branch of methane raw material gas, a second branch of methane raw material gas and a third branch of methane raw material gas, wherein the methane raw material gas in the first branch of methane raw material gas and the flue gas to be treated in the flue gas pipeline to be treated are mixed and then enter a methane lean-oxygen combustion reaction device for catalytic combustion to generate carbon monoxide and hydrogen, and then the carbon monoxide and the hydrogen, together with the unreacted methane raw material gas and the flue gas to be treated, are mixed with methane in the second branch of methane raw material gas and then enter a flue gas desulfurization and denitrification reaction device for flue gas desulfurization and denitrification reaction under the action of a catalyst; the flue gas after desulfurization and denitrification carries part of catalyst to enter a cyclone separator, the separated high-temperature sulfur-containing elemental flue gas enters a cooling tower to be cooled, then enters a heat exchanger to exchange heat with methane raw material gas in a methane raw material gas pipeline, and then is discharged out of the system, and the cooling tower obtains sulfur;
and the catalyst after reaction in the flue gas desulfurization and denitration reaction device, the catalyst separated by the cyclone separator and the methane feed gas in the third branch of the methane feed gas enter a catalyst regenerator for regeneration and then enter the flue gas desulfurization and denitration reaction device again for the next round of reaction.
Preferably, the molar ratio of the methane raw material gas in the methane lean-oxygen combustion reaction device to the oxygen in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-50000 h-1The reaction temperature is 250-350 ℃.
Preferably, the pollutants in the flue gas to be treated comprise SO2、NO、N2O、N2O3、N2O4，N2O5And NO2The total concentration of pollutants is 2000-20000 ppm, and the content of oxygen in the flue gas to be treated is 1% -6%.
Further preferably, the molar ratio of the methane raw gas in the flue gas desulfurization and denitrification reaction device to the total amount of pollutants in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-20000 h-1The reaction temperature is 450-650 ℃.
Compared with the prior art, the invention has the following beneficial technical effects:
according to the system for performing the flue gas desulfurization and denitrification by using the methane, the desulfurization and denitrification catalytic reaction needs to be performed under the anaerobic condition, so that before the flue gas desulfurization and denitrification reaction, the flue gas is firstly subjected to deoxidation treatment in a methane lean-oxygen combustion reaction device, then, sulfur oxides and the methane in the flue gas react in a fluidized bed reactor in the presence of a catalyst to generate elemental sulfur, nitrogen oxides generate nitrogen, and the methane is converted into carbon dioxide and water vapor. The system has reasonable structural design, wide sources of methane as a reducing agent, low cost and convenient storage and use; the desulfurization and denitrification are carried out simultaneously, the pollutant treatment efficiency is improved, the recycling of sulfur element can be realized, waste is changed into valuable, other waste residues and waste liquid are not generated, no secondary pollution is caused, the environment friendliness is realized, and economic benefits are brought.
Furthermore, the plug valve can be used for controlling the circulation amount of the catalyst, so that the reaction rate of the whole system can be controlled.
Furthermore, the catalysts in the methane lean-oxygen combustion reaction device and the flue gas desulfurization and denitration reaction device adopt supported metal catalysts which are commonly used in the industry, the preparation process is mature, the wear resistance of the catalysts can be improved by adding a carrier, and the catalysts are good in adjustability and degeneration and can be suitable for flue gas treatment processes with different components; good fluidization property, suitability for a fluidized bed reactor, mild regeneration condition, good carbon deposition resistance and sulfur resistance of the catalyst, and long service life.
Furthermore, the catalyst of the supported metal oxide catalyst is one or more of simple substances of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium, the carrier is one or more of oxides of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium, the screening and proportioning of the catalyst carrier and active components can be adjusted according to the components of the flue gas and the desulfurization and denitrification effects, and the flexibility is high.
Furthermore, the methane lean-oxygen combustion reaction device adopts a fixed bed reactor, and the flue gas desulfurization and denitrification reaction device adopts a fluidized bed reactor, so that the reaction efficiency is high, and the operation is simple and convenient.
According to the method for performing desulfurization and denitrification on the flue gas by using the system, after the flue gas is subjected to deoxidation reaction, sulfur oxides and methane in the flue gas are subjected to desulfurization and denitrification reaction in the presence of a catalyst to generate elemental sulfur, nitrogen oxides generate nitrogen, and the methane is converted into carbon dioxide and water vapor. The method is simple to operate, can effectively remove sulfur oxides and nitrogen oxides in the flue gas, can change waste into valuables to produce sulfur products, and has good economic benefit and market application prospect.
Further, the molar ratio of the methane raw material gas in the methane lean-oxygen combustion reaction device to the oxygen in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-50000 h-1The reaction temperature is 250-350 ℃, under the parameters, the catalyst activity is high, the oxygen removal efficiency is high, the flue gas treatment capacity is large, and the reaction conditions can be matched with the preorder flow of a factory. Further, the pollutants in the flue gas to be treated comprise SO2、NO、N2O、N2O3、N2O4，N2O5And NO2The total concentration of the pollutants is 2000-20000 ppm, the content of oxygen is 1% -6%, the gases containing sulfur oxides and nitrogen oxides can be treated simultaneously, the applicable pollutant concentration range is wide, the removal rate of various sulfur oxides and nitrogen oxides with different concentrations is high, and the method is applicable to factory flue gas treatment processes with different production conditions.
Further, the molar ratio of the methane feed gas in the flue gas desulfurization and denitrification reaction device to the total amount of pollutants in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-20000 h-1The reaction temperature is 450-650 ℃, under the reaction condition, the catalyst activity is high, the oxygen removal efficiency is high, the flue gas treatment capacity is large, and the reaction condition is also suitable for being combined with the previous process.
Drawings
FIG. 1 is a schematic view of the whole system for desulfurization and denitrification of flue gas by using methane according to the present invention.
In the figure: 1-methane lean oxygen combustion reaction device, 2-flue gas desulfurization and denitration reaction device, 3-catalyst regenerator, 4-cyclone separator, 5-cooling tower, 6-heat exchanger, 7-sulfur bin, 8-plug valve; 10-a methane raw material gas pipeline, 11-a flue gas pipeline to be treated, 12-a mixed gas pipeline, 101-a methane raw material gas first branch, 102-a methane raw material gas second branch, 103-a methane raw material gas third branch, 23-a catalyst regeneration first pipeline, 24-a treated flue gas pipeline, 32-a regenerated catalyst pipeline, 43-a catalyst regeneration second pipeline, 45-a sulfur-containing elemental flue gas pipeline, 56-a sulfur-removing flue gas pipeline, 57-solid sulfur and 70-a sulfur product.
Detailed Description
The invention will now be described in further detail with reference to the following drawings and specific examples, which are intended to be illustrative and not limiting:
FIG. 1 is a system for desulfurization and denitrification of flue gas by using methane, which comprises a methane lean-oxygen combustion reaction device 1, a flue gas desulfurization and denitrification reaction device 2, a catalyst regenerator 3, a cyclone separator 4, a cooling tower 5 and a heat exchanger 6;
an inlet of the methane lean-oxygen combustion reaction device 1 is connected with a flue gas pipeline 11 to be treated and a first branch 101 of a methane raw gas, an outlet of the methane lean-oxygen combustion reaction device 1 is connected with a gas inlet of a flue gas desulfurization and denitration reaction device 2 through a mixed gas pipeline 12, the gas inlet of the flue gas desulfurization and denitration reaction device 2 is also connected with a second branch 102 of the methane raw gas, a solid outlet of the flue gas desulfurization and denitration reaction device 2 is connected with a solid inlet of a catalyst regenerator 3 through a first catalyst regeneration pipeline 23, and the first catalyst regeneration pipeline 23 is provided with a plug valve 8 for controlling the circulation amount of a catalyst; a gas outlet of the flue gas desulfurization and denitration reaction device 2 is connected with an inlet of a cyclone separator 4 through a treated flue gas pipeline 24, an outlet of a catalyst regenerator 3 is connected with a gas inlet of the flue gas desulfurization and denitration reaction device 2 through a regenerated catalyst pipeline 32, a catalyst is brought into the flue gas desulfurization and denitration reaction device 2 by a mixed gas in a mixed gas pipeline 12 and a methane gas in a methane raw gas second branch 102, a solid outlet of the cyclone separator 4 is connected with a solid inlet of the catalyst regenerator 3 through a catalyst regeneration second pipeline 43, and a gas inlet of the catalyst regenerator 3 is connected with a methane raw gas third branch 103; the gas outlet of the cyclone separator 4 is connected with the inlet of the cooling tower 5 through a sulfur-containing elementary gas flue gas pipeline 45, the gas outlet of the cooling tower 5 is connected with the heat exchanger 6 through a sulfur-removing flue gas pipeline 56, the heat exchanger 6 is connected with a methane raw gas pipeline 10, and the methane raw gas pipeline 10 is connected with a methane raw gas first branch 101, a methane raw gas second branch 102 and a methane raw gas third branch 103.
The methane lean-oxygen combustion reaction device 1 preferably adopts a fixed bed reactor, and the flue gas desulfurization and denitrification reaction device 2 preferably adopts a fluidized bed reactor.
The catalysts in the methane lean-oxygen combustion reaction device 1 and the flue gas desulfurization and denitration reaction device 2 adopt supported metal oxide catalysts, the catalysts are one or more of simple substances of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium, and the carriers are one or more of oxides of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium.
The method for performing flue gas desulfurization and denitration by using methane comprises the following steps:
the pollutants in the smoke to be treated of the object comprise SO2、NO、N2O、N2O3、N2O4，N2O5And NO2The total concentration of pollutants is 2000-20000 ppm, and the content of oxygen in the flue gas to be treated is 1% -6%.
The methane raw material gas in the methane raw material gas pipeline 10 is divided into a first methane raw material gas branch 101, a second methane raw material gas branch 102 and a third methane raw material gas branch 103, wherein the methane raw material gas in the first methane raw material gas branch 101 and the flue gas to be treated in the flue gas pipeline 11 to be treated are mixed and then enter a methane lean-oxygen combustion reaction device 1 for catalytic combustion, the molar ratio of the methane raw material gas to the oxygen in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-50000 h-1The reaction temperature is 250-350 ℃, after carbon monoxide and hydrogen are generated, the carbon monoxide and the hydrogen together with the unreacted methane feed gas and the flue gas to be treated are mixed with methane in the second branch 102 of the methane feed gas and then enter a flue gas desulfurization and denitrification reaction device 2, the flue gas desulfurization and denitrification reaction is carried out under the action of a catalyst, the molar ratio of the methane feed gas in the flue gas desulfurization and denitrification reaction device to the total amount of pollutants in the flue gas to be treated is 0.5-2: 1, and the reaction airspeed is 5000-20000 h-1The reaction temperature is 450-650 ℃; the flue gas after desulfurization and denitrification carries part of catalyst to enter a cyclone separator 4, the separated high-temperature sulfur-containing simple substance flue gas enters a cooling tower 5 to be cooled and then enters a heat exchanger 6 and a methane raw material gas pipeline 10And (3) discharging the alkane feed gas after heat exchange to a system, adopting a flue gas analyzer to analyze the concentration of sulfur oxides and nitrogen oxides in the treated flue gas on line, calculating the removal rate, and adjusting the reaction parameters of the system in real time according to the result, wherein the higher the removal rate is, the better the effect is. The solid sulfur 57 obtained from the cooling tower 5 enters a sulfur bunker 7 for collection and treatment to obtain a sulfur product 70.
The catalyst after the reaction in the flue gas desulfurization and denitration reaction device 2, the catalyst separated by the cyclone separator 4 and the methane feed gas in the third branch 103 of the methane feed gas enter the catalyst regenerator 3 for regeneration and then enter the flue gas desulfurization and denitration reaction device 2 again for the next round of reaction.
The effects of the present invention are further verified with reference to the following examples:
example 1
With a NO concentration of 1200ppm and SO2The simulated flue gas with the concentration of 1000ppm, 4 percent of oxygen and the balance of nitrogen is reacted, the flue gas deoxidation is carried out by adopting cerium oxide to load metal palladium, the flue gas desulfurization and denitrification reaction adopts alumina as a carrier and cerium oxide as an active component, the reaction is carried out, and the deoxidation reaction airspeed is 5000h-1The temperature is 250 ℃, and the air speed of the flue gas desulfurization and denitrification reaction is 5000-20000 h-1The reaction temperature was 550 ℃. The catalyst regeneration reaction temperature is 500 ℃. The pollutant removal rate at the airspeed of the flue gas desulfurization and denitrification reaction is shown in Table 1, and the visible airspeed is 10000h-1The removal effect is best.
TABLE 1 contaminant removal Rate at different space velocities
Figure BDA0002255577890000071
Example 2
With a NO concentration of 1200ppm and SO2The simulated flue gas with the concentration of 1000ppm, 4 percent of oxygen and the balance of nitrogen is reacted, the flue gas deoxidation is carried out by adopting cerium oxide to load metal palladium, the flue gas desulfurization and denitrification reaction adopts alumina as a carrier and cerium oxide as an active component to carry out the reaction, and the deoxidation reaction airspeed is 20000h-1At 300 deg.C, desulfurizing fumeThe denitration reaction space velocity is 10000h-1The reaction temperature is 450-650 ℃. The catalyst regeneration reaction temperature is 500 ℃. The pollutant removal rate at the airspeed of the flue gas desulfurization and denitrification reaction is shown in table 2, and the removal effect is better when the temperature is higher than 550 ℃.
TABLE 2 removal rate of pollutants at different reaction temperatures for desulfurization and denitrification of flue gas
Figure BDA0002255577890000081
Example 3
With a NO concentration of 1200ppm and SO2The simulated flue gas with the concentration of 1000ppm, 4 percent of oxygen and the balance of nitrogen is reacted, the flue gas deoxidation is carried out by adopting cerium oxide to load metal palladium, the flue gas desulfurization and denitrification reaction adopts alumina as a carrier and cerium oxide as an active component to carry out the reaction, and the deoxidation reaction airspeed is 20000h-1The temperature is 350 ℃, and the space velocity of the flue gas desulfurization and denitrification reaction is 10000h-1The reaction temperature was 550 ℃. The regeneration reaction temperature of the catalyst is 400-600 ℃. The pollutant removal rate at the airspeed of the flue gas desulfurization and denitrification reaction is shown in table 3, and the removal effect is better when the temperature is 500 ℃.
TABLE 3 removal of contaminants at different regeneration temperatures
Figure BDA0002255577890000082
Example 4
By containing SO2、NO、N2O、N2O3、N2O4，N2O5And NO2The concentration of the simulated flue gas is 1000ppm, 4% of oxygen and the balance of nitrogen are reacted, the flue gas deoxidation adopts cerium oxide to load metal palladium for reaction, the flue gas desulfurization and denitration reaction adopts alumina as a carrier and cerium oxide as an active component for reaction, and the space velocity of the deoxidation reaction is 20000h-1The temperature is 300 ℃, and the space velocity of the flue gas desulfurization and denitrification reaction is 10000h-1The reaction temperature was 550 ℃. The catalyst regeneration reaction temperature is 500 ℃, and the pollutant removal rate is highAll reach more than 95 percent.
Example 5
With a NO concentration of 1200ppm and SO2The simulated flue gas with the concentration of 1000ppm, 4 percent of oxygen and the balance of nitrogen is reacted, the flue gas deoxidation adopts cerium oxide loaded metal palladium for reaction, catalysts with different components are adopted for desulfurization and denitrification reaction, and the deoxidation reaction airspeed is 20000h-1The temperature is 300 ℃, and the space velocity of the flue gas desulfurization and denitrification reaction is 10000h-1The reaction temperature was 550 ℃. The catalyst regeneration reaction temperature is 500 ℃. The pollutant removal rate at the airspeed of the flue gas desulfurization and denitration reaction is shown in table 5, and the best effect is achieved when the alumina is used as a carrier and the cerium oxide is used as an active component for desulfurization and denitration reaction.
TABLE 5-1 pollutant removal rates under catalysis of different desulfurization and denitrification catalysts
Figure BDA0002255577890000091
TABLE 5-2 pollutant removal rates under catalysis of different desulfurization and denitrification catalysts
TABLE 5-3 pollutant removal rates under catalysis of different desulfurization and denitrification catalysts
Figure BDA0002255577890000093
Figure BDA0002255577890000101
TABLE 5-4 pollutant removal rate under catalysis of different desulfurization and denitrification catalysts
Figure BDA0002255577890000102
It should be noted that the above description is only one embodiment of the present invention, and all equivalent changes of the system described in the present invention are included in the protection scope of the present invention. Persons skilled in the art to which this invention pertains may substitute similar alternatives for the specific embodiments described, all without departing from the scope of the invention as defined by the claims.

Claims (10)

1. A system for flue gas desulfurization and denitration by using methane is characterized by comprising a methane lean-oxygen combustion reaction device (1), a flue gas desulfurization and denitration reaction device (2), a catalyst regenerator (3), a cyclone separator (4), a cooling tower (5) and a heat exchanger (6);
an inlet of the methane lean-oxygen combustion reaction device (1) is connected with a flue gas pipeline (11) to be treated and a first branch (101) of a methane raw gas, an outlet of the methane lean-oxygen combustion reaction device (1) is connected with an inlet of the flue gas desulfurization and denitration reaction device (2), an inlet of the flue gas desulfurization and denitration reaction device (2) is also connected with a second branch (102) of the methane raw gas, and a solid outlet of the flue gas desulfurization and denitration reaction device (2) is connected with a solid inlet of a catalyst regenerator (3); a gas outlet of the flue gas desulfurization and denitration reaction device (2) is connected with an inlet of a cyclone separator (4), an outlet of a catalyst regenerator (3) is connected with an inlet of the flue gas desulfurization and denitration reaction device (2), a solid outlet of the cyclone separator (4) is connected with a solid inlet of the catalyst regenerator (3), and a gas inlet of the catalyst regenerator (3) is connected with a third branch (103) of methane feed gas; the gas outlet of the cyclone separator (4) is connected with the inlet of the cooling tower (5), the gas outlet of the cooling tower (5) is connected with the heat exchanger (6), the heat exchanger (6) is connected with a methane raw material gas pipeline (10), and the methane raw material gas pipeline (10) is connected with a methane raw material gas first branch (101), a methane raw material gas second branch (102) and a methane raw material gas third branch (103).
2. The system for flue gas desulfurization and denitration by methane according to claim 1, wherein a plug valve (8) is provided on a connecting line between the solid outlet of the flue gas desulfurization and denitration reaction device (2) and the solid inlet of the catalyst regenerator (3).
3. The system for flue gas desulfurization and denitration using methane according to claim 1, wherein the catalyst in the methane lean-oxygen combustion reaction device (1) and the flue gas desulfurization and denitration reaction device (2) is a supported metal oxide catalyst.
4. The system for flue gas desulfurization and denitration by methane according to claim 3, wherein the catalyst of the supported metal oxide catalyst is one or more of the simple substances of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium, and the carrier is one or more of the oxides of aluminum, magnesium, iron, cerium, calcium, palladium, copper, nickel, lanthanum and vanadium.
5. The system for flue gas desulfurization and denitration by methane according to claim 1, wherein the methane lean-oxygen combustion reaction device (1) is a fixed bed reactor.
6. The system for flue gas desulfurization and denitration by methane according to claim 1, wherein the flue gas desulfurization and denitration reaction device (2) is a fluidized bed reactor.
7. The method for performing flue gas desulfurization and denitration by using methane according to any one of claims 1 to 6, characterized by comprising:
the methane raw material gas in the methane raw material gas pipeline (10) is divided into a methane raw material gas first branch (101), a methane raw material gas second branch (102) and a methane raw material gas third branch (103), wherein the methane raw material gas in the methane raw material gas first branch (101) and the flue gas to be treated in the flue gas pipeline to be treated (11) are mixed and then enter a methane lean-oxygen combustion reaction device (1) for catalytic combustion to generate carbon monoxide and hydrogen, and then the carbon monoxide and the hydrogen are mixed with the unreacted methane raw material gas and the flue gas to be treated and enter a flue gas desulfurization and denitrification reaction device (2) after being mixed with the methane in the methane raw material gas second branch (102), and flue gas desulfurization and denitrification reaction are carried out under the action of a catalyst; the flue gas after desulfurization and denitrification carries part of catalyst to enter a cyclone separator (4), the separated high-temperature sulfur-containing elementary substance flue gas enters a cooling tower (5) to be cooled, then enters a heat exchanger (6) to exchange heat with methane raw material gas in a methane raw material gas pipeline (10), and then is discharged out of the system, and sulfur is obtained by the cooling tower (5);
the catalyst after reaction in the flue gas desulfurization and denitration reaction device (2), the catalyst separated by the cyclone separator (4) and the methane feed gas in the third branch (103) of the methane feed gas enter the catalyst regenerator (3) for regeneration and then enter the flue gas desulfurization and denitration reaction device (2) again for the next round of reaction.
8. The method for flue gas desulfurization and denitration by using methane as claimed in claim 7, wherein the molar ratio of the methane feed gas in the methane lean-oxygen combustion reaction device (1) to the oxygen in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-50000 h-1The reaction temperature is 250-350 ℃.
9. The method for desulfurization and denitrification of flue gas by using methane according to claim 7, wherein the pollutants in the flue gas to be treated comprise SO2、NO、N2O、N2O3、N2O4，N2O5And NO2The total concentration of pollutants is 2000-20000 ppm, and the content of oxygen in the flue gas to be treated is 1% -6%.
10. The method for flue gas desulfurization and denitration by using methane according to claim 9, wherein the molar ratio of the methane raw gas in the flue gas desulfurization and denitration reaction device (2) to the total amount of pollutants in the flue gas to be treated is 0.5-2: 1, and the reaction space velocity is 5000-20000 h-1The reaction temperature is 450-650 ℃.
CN201911052117.3A 2019-10-31 2019-10-31 System and method for flue gas desulfurization and denitration by using methane Pending CN110694470A (en)

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CN101094805A (en) * 2004-11-09 2007-12-26 弗劳尔科技公司 Configurations and methods for sox removal in oxygen-containing gases
CN102895872A (en) * 2011-07-28 2013-01-30 中国石油化工股份有限公司 Method for removing sulfur oxides and nitrogen oxides in catalytic cracking regeneration flue gas
CN210934478U (en) * 2019-10-31 2020-07-07 中国华能集团有限公司 System for flue gas desulfurization and denitration are carried out with methane

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CN101094805A (en) * 2004-11-09 2007-12-26 弗劳尔科技公司 Configurations and methods for sox removal in oxygen-containing gases
CN102895872A (en) * 2011-07-28 2013-01-30 中国石油化工股份有限公司 Method for removing sulfur oxides and nitrogen oxides in catalytic cracking regeneration flue gas
CN210934478U (en) * 2019-10-31 2020-07-07 中国华能集团有限公司 System for flue gas desulfurization and denitration are carried out with methane

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112516736A (en) * 2020-12-02 2021-03-19 南通斐腾新材料科技有限公司 Denitration process and denitration equipment

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