CN109569251B - By using a gas containing SO2Device and method for preparing dilute sulfuric acid from flue gas - Google Patents

By using a gas containing SO2Device and method for preparing dilute sulfuric acid from flue gas Download PDF

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CN109569251B
CN109569251B CN201910045641.1A CN201910045641A CN109569251B CN 109569251 B CN109569251 B CN 109569251B CN 201910045641 A CN201910045641 A CN 201910045641A CN 109569251 B CN109569251 B CN 109569251B
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hydrogen peroxide
sulfuric acid
dilute sulfuric
supergravity
gas
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CN109569251A (en
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张亮亮
董宇宁
陈建峰
初广文
邹海魁
孙宝昌
罗勇
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Beijing University of Chemical Technology
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/507—Sulfur oxides by treating the gases with other liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8609—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D53/86—Catalytic processes
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Abstract

The invention discloses a method for utilizing SO-containing gas2The process method for preparing dilute sulfuric acid from flue gas comprises a cooling and dedusting device, a supergravity absorption device, a defoaming device, a rich liquid storage tank, a rich liquid delivery pump, a rich liquid flow regulating valve, a dilute sulfuric acid flow regulating valve, a supergravity reduction device, a hydrogen peroxide storage tank, a hydrogen peroxide delivery pump and a hydrogen peroxide flow regulating valve which are connected in a certain mode2The deep removal improves the concentration of the produced dilute sulfuric acid, and the catalyst is loaded on the filler to form a supergravity reduction device, so that the hydrogen peroxide in the dilute sulfuric acid product is effectively decomposed. The invention can realize SO2The deep removal of the sulfur, the effective recovery of sulfur resources, and the by-product of high-quality dilute sulfuric acid are suitable for SO-containing flue gas of alkylation plants, sulfuric acid plants and the like2And (4) treating industrial flue gas.

Description

By using a gas containing SO2Device and method for preparing dilute sulfuric acid from flue gas
Technical Field
The invention relates to a method for utilizing SO in flue gas2Device and method for preparing dilute sulfuric acid product and realizing SO2And the high-quality dilute sulfuric acid is produced as a byproduct during deep removal.
Background
Sulfur dioxide (SO)2) Is one of the main atmospheric pollutants, SO2Excessive discharge can cause serious harm to human health and ecological environment. In recent years, the industry of China has developed rapidly, SO2The emission level is about 2000 million tons/year for controlling SO2Discharge of pollutants, much SO2The application of the removal technology is not without fail, and at present,the industrial sulfur-containing tail gas treatment method mainly comprises a limestone-gypsum method, an ammonia method, a calcium-sodium alkaline method and the like, and the desulfurization technologies can realize high SO2The removal efficiency is high, but simultaneously desulfurization waste is generated, the treatment difficulty is high, and secondary pollution is caused to the environment.
The hydrogen peroxide desulfurization method is one of wet desulfurization techniques developed in recent years and has the principle that SO2Is oxidized by hydrogen peroxide to generate dilute sulfuric acid which is an important basic chemical raw material and is widely applied in industrial processes such as metallurgy, alkylation and the like, SO that the byproduct sulfuric acid product generated by desulfurization by using the hydrogen peroxide is used for controlling SO2An efficient method for achieving sulfur resource recycling while discharging. For the hydrogen peroxide desulfurization process, SO2The higher the removal efficiency, the higher the concentration of the dilute sulfuric acid product, and the lower the content of residual hydrogen peroxide, the better the desulfurization process effect. The prior patent relating to the hydrogen peroxide desulfurization technology still has certain problems in process design or process effect. In patent CN 105749715 a and CN 104671221 a, a hydrogen peroxide solution desulfurization mechanism and a device connection manner are described, but there are certain disadvantages that, on one hand, the desulfurization device adopts the form of traditional tower type devices, such as a packed tower, a fixed bed, etc., the power source in which the fluid flows is gravity, and the mass transfer separation efficiency in these devices is influenced by gravity, resulting in SO2The deep removal is difficult, the concentration of the produced dilute sulfuric acid product is low, and the residual hydrogen peroxide is difficult to be deeply decomposed by the hydrogen peroxide reduction device due to the gravity limitation, so that the residual amount of the hydrogen peroxide in the dilute sulfuric acid product is large; in the process flow, the newly added hydrogen peroxide and the desulfurization rich liquid are mixed and then do not contact with the sulfur-containing gas firstly, but pass through a flow path of circular extraction firstly, so that the fresh hydrogen peroxide is likely to be extracted directly into a dilute sulfuric acid product without contacting with the sulfur-containing gas, and the waste of the hydrogen peroxide and the difficulty in decomposition of the hydrogen peroxide in the dilute sulfuric acid product are increased. In addition, other patents relating to hydrogen peroxide desulfurization have defects in process effect, and patents CN 106606924A and CN 205627604A disclose methods and devices for hydrogen peroxide desulfurization, but the concentration of the by-product dilute sulfuric acid product is below 30 w%; CN 202070285U discloses a method for removing sulfuric acid industrial tailSulfur dioxide in the gas, a device for recovering sulfuric acid, and the sulfur dioxide content in the treated tail gas still is 40-60 mg/m3(ii) a CN 100354028C discloses a method for removing sulfur dioxide from waste gas by reaction with hydrogen peroxide, and 500ppm hydrogen peroxide still remains in the produced dilute sulfuric acid. Based on the problems of the existing hydrogen peroxide desulfurization technology, the invention provides a method for utilizing SO-containing gas2The device and the method for preparing dilute sulfuric acid by using the flue gas can realize SO2The deep removal of the sulfur, the effective utilization of sulfur resources, and the by-product of dilute sulfuric acid with higher concentration and less residual amount of hydrogen peroxide.
Disclosure of Invention
The invention aims to remove SO contained in industrial process flue gas2Deeply removing, recovering sulfur resources and producing high-quality dilute sulfuric acid as a byproduct, specifically:
the invention relates to a method for utilizing SO-containing gas2The device for preparing dilute sulfuric acid by using flue gas comprises: (1) the device comprises a cooling and dedusting device, (2) a supergravity absorption device, (3) a defoaming device, (4) a rich liquid storage tank, (5) a rich liquid delivery pump, (6) a rich liquid flow regulating valve, (7) a dilute sulfuric acid flow regulating valve, (8) a supergravity reduction device, (9) a hydrogen peroxide storage tank, (10) a hydrogen peroxide delivery pump, and (11) a hydrogen peroxide flow regulating valve. The gas outlet of the cooling and dedusting device is connected with a gas inlet of the supergravity absorption device (2), a gas outlet of the supergravity absorption device (2) is connected with a defoaming device (3), a liquid outlet of the defoaming device (3) is connected with a liquid inlet pipeline of the supergravity absorption device (2), a liquid outlet of the hydrogen peroxide storage tank (9) is connected with a liquid inlet pipeline of the supergravity absorption device (2) through a hydrogen peroxide delivery pump (10) and a hydrogen peroxide flow regulating valve (11), a liquid outlet pipeline of the supergravity absorption device (2) is connected with a rich liquid storage tank (4), a liquid outlet of the rich liquid storage tank (4) is connected with two branches through a rich liquid delivery pump (5), one is connected with a liquid inlet pipeline of the supergravity absorption device (2) through a rich liquid flow regulating valve (6), and the other is connected with a dilute sulfuric acid flow regulating valve (7) and a supergravity reduction device (8) to serve as a product extraction line.
The invention provides the use of the above-mentioned apparatus for the utilization of SO-containing gases2The method for preparing dilute sulfuric acid by using flue gas specifically comprises the following steps:
(1) containing SO2The flue gas enters a temperature-reducing and dust-removing device, the temperature is reduced, and solid impurities carried in the flue gas are removed;
(2) the gas cooled and dedusted in the step (1) enters a supergravity absorption device and contacts with absorbent hydrogen peroxide solution in the supergravity absorption device, and SO2Entering a liquid phase to form hydrogen peroxide mixed absorption liquid containing sulfuric acid, entering the desulfurized gas into a defoaming device to remove entrained absorption liquid, discharging the gas from a chimney or sending the gas to a downstream process, and returning the removed entrained absorption liquid to the supergravity absorption device;
(3) enabling the absorption rich solution subjected to desulfurization in the step (2) to enter a rich solution storage tank, circularly absorbing the rich solution in the rich solution storage tank through a rich solution delivery pump and a flow regulating valve, and extracting the rich solution through a dilute sulfuric acid flow regulating valve when the concentration of dilute sulfuric acid in the rich solution reaches a specified concentration;
(4) after the dilute sulfuric acid reaches the specified concentration in the step (3), extracting the dilute sulfuric acid by a dilute sulfuric acid flow regulating valve, feeding the dilute sulfuric acid into a supergravity reduction device, loading a hydrogen peroxide reduction catalyst on a filler used by the supergravity reduction device, removing residual hydrogen peroxide in the extracted dilute sulfuric acid under the action of the catalyst, and collecting or sending the dilute sulfuric acid to a downstream process as a product;
(5) the hydrogen peroxide storage tank stores hydrogen peroxide with a certain concentration, and when the desulfurization absorption liquid detects that the concentration of the hydrogen peroxide is too low, the hydrogen peroxide delivery pump and the hydrogen peroxide flow regulating valve can be used for timely supplementing the absorbent.
Preferably, the temperature of the flue gas after temperature reduction and dust removal in the step (1) is controlled to be 15-50 ℃.
Preferably, the supergravity absorption device in step (2) is selected from supergravity rotating devices including, but not limited to, rotating packed beds, baffled type, stator-rotor type and the like.
Preferably, in the step (2), the pressure in the supergravity absorption device is 0.05-0.5 MPa, the temperature is 15-50 ℃, the initial concentration of the absorbent is 0.1-8 w%, the supergravity level of the supergravity absorption device is 80-200, and the gas-liquid volume flow rate ratio in the supergravity absorption device is 200-650.
Preferably, the mass fraction of the dilute sulfuric acid product in the step (3) is 20-55%.
Preferably, the filler used in step (4) supports a hydrogen peroxide reduction catalyst, including but not limited to MnO2And CuO, Pt, Ag, Cr and other catalysts, wherein the load of the catalysts is 2-10 v%, and the hypergravity level of the hypergravity reduction device is 90-180%.
The invention can realize the following beneficial effects:
the invention uses the supergravity absorption device as the core equipment and can strengthen SO2Gas-liquid mass transfer process with hydrogen peroxide system, and gas outlet SO of supergravity absorption device2The concentration can be reduced to 25mg/m3The sulfur resource almost enters into the dilute sulfuric acid product to realize SO2Deep removal and effective utilization of sulfur resources; due to SO2The removal efficiency is high, the dilute sulfuric acid can be extracted at a higher concentration of more than 40 w%, and the difficulty of refining the dilute sulfuric acid into concentrated sulfuric acid is reduced; the process adopts a supergravity reduction device to reduce MnO2When the hydrogen peroxide decomposition catalyst is loaded on the filler of the supergravity reduction device, the filler crushes the liquid phase, more areas are exposed to be contacted with the catalyst, the concentration of residual hydrogen peroxide in the dilute sulfuric acid product can be reduced to be below 300ppb, and the quality of the dilute sulfuric acid product is improved. Meanwhile, no pollution waste is generated, the process is simple, the installation is convenient, and the method is suitable for the tail gas containing SO such as the alkylation tail gas, the tail gas of the sulfuric acid plant and the like2The industrial flue gas treatment process.
Drawings
FIG. 1 shows a process for producing a compound containing SO according to the present invention2The flue gas produces the schematic view of the apparatus of dilute sulphuric acid.
In fig. 1: the method comprises the following steps of 1-cooling and dedusting device, 2-hypergravity absorption device, 3-defoaming device, 4-rich liquid storage tank, 5-rich liquid delivery pump, 6-rich liquid flow regulating valve, 7-dilute sulfuric acid flow regulating valve, 8-hypergravity reduction device, 9-hydrogen peroxide storage tank, 10-hydrogen peroxide delivery pump and 11-hydrogen peroxide flow regulating valve.
Detailed Description
Referring to the drawings, embodiments of the present invention will be further described with reference to the drawings and examples.
Apparatus and method for using the inventionBy using gases containing SO2The process method for preparing dilute sulfuric acid by using flue gas comprises the following steps: containing SO2The flue gas firstly enters a cooling and dedusting device, the temperature of the flue gas is reduced within a proper range, solid impurities contained in the flue gas are removed, the flue gas after cooling and dedusting enters a supergravity absorption device, the flue gas is contacted with a hydrogen peroxide solution with a certain initial concentration in the supergravity absorption device, and SO in the flue gas2The flue gas is absorbed and enters a liquid phase, the desulfurized flue gas leaves from a gas outlet of the supergravity absorption device, the flue gas is sent to a downstream process after entrained absorption liquid is removed by a defoaming device, the entrained absorption liquid returns to the supergravity absorption device, the desulfurized rich solution enters a rich solution storage tank, the rich solution in the rich solution storage tank is recycled by a rich solution delivery pump and a rich solution flow regulating valve, the rich solution can be extracted by a dilute sulfuric acid flow regulating valve after the concentration of sulfuric acid in the rich solution reaches a certain concentration, the extracted dilute sulfuric acid is removed with a small amount of residual hydrogen peroxide by a supergravity reduction device, and then the dilute sulfuric acid is collected as a dilute sulfuric acid product or sent to the downstream process.
Example 1
Utilizing SO-containing gas using the above apparatus and method2The flue gas is used for preparing dilute sulfuric acid. The temperature for cooling and dedusting the flue gas is controlled at 25 ℃, the temperature of the supergravity absorption device is controlled at 25 ℃, the pressure is 0.1MPa, the initial concentration of hydrogen peroxide is 2 w%, the supergravity level is 100, the volumetric flow ratio of gas and liquid in the supergravity absorption device is controlled at 450, the mass fraction of dilute sulfuric acid products is controlled at 45 w%, the load of a catalyst used for reducing the hydrogen peroxide is 5 v%, and the supergravity level of the supergravity reduction device is 120.
Gas sample analysis, SO, at the gas outlet of the demister2The concentration is 15mg/m3And sampling and analyzing at the outlet of the supergravity reduction device, wherein the content of hydrogen peroxide in the dilute sulfuric acid product is 280 ppb.
Examples 2 to 25
The technological process and steps are the same as those of the example 1, the temperature, the pressure, the hydrogen peroxide concentration, the hypergravity level of the hypergravity absorption device and the hypergravity reduction device, the hydrogen peroxide reduction catalyst loading capacity, the gas-liquid volume flow ratio in the hypergravity absorption device, the dilute sulfuric acid concentration and the gas outlet SO of the defoaming device in each example2Concentration ofThe results of the hydrogen peroxide content in the dilute sulfuric acid product are shown in table 1.
TABLE 1 Process conditions and Experimental results for the examples
Figure BDA0001949065430000051
Note: t is1-the temperature of the flue gas after cooling and dedusting; t is2-supergravity absorption device temperature; p1-supergravity absorber pressure;
initial concentration of omega hydrogen peroxide-hydrogen peroxide; beta is a1-the level of supergravity of the supergravity absorption means; G/L-gas-liquid volume flow ratio;
controlling the concentration of omega dilute sulfuric acid-dilute sulfuric acid; beta is a2-the hypergravity level of the hypergravity reduction device;
Figure BDA0001949065430000052
hydrogen peroxide reduction catalyst loading;
SO2concentration-SO in the outlet gas of the demister2Concentration; the content of hydrogen peroxide in C hydrogen peroxide-dilute sulphuric acid product
Comparative examples 1 to 12
The process flow and the steps are the same as those of the example 1, the temperature, the pressure, the hydrogen peroxide concentration, the hypergravity level of the hypergravity absorption device and the hypergravity reduction device, the load of the hydrogen peroxide reduction catalyst, the gas-liquid volume flow ratio in the hypergravity absorption device, the concentration of the dilute sulfuric acid and the SO outlet of the defoaming device in all proportions are respectively matched2The results of concentration and hydrogen peroxide content in the dilute sulfuric acid product are shown in table 2.
TABLE 2 Process conditions and Experimental results for each comparative example
Figure BDA0001949065430000061
Note: t is1-the temperature of the flue gas after cooling and dedusting; t is2-supergravity absorption device temperature; p1-supergravity absorber pressure;
omega hydrogen peroxide-hydrogen peroxideAn initial concentration; beta is a1-the level of supergravity of the supergravity absorption means; G/L-gas-liquid volume flow ratio;
controlling the concentration of omega dilute sulfuric acid-dilute sulfuric acid; beta is a2-the hypergravity level of the hypergravity reduction device;
Figure BDA0001949065430000062
-hydrogen peroxide reduction catalyst loading;
SO2concentration-SO in the outlet gas of the demister2Concentration; the content of hydrogen peroxide in C hydrogen peroxide-dilute sulphuric acid product
Comparative example 13
As described in example 1, the supergravity absorber was changed to a packed column with the same packing volume, except that the conditions were not changed.
Gas sample analysis, SO, at the gas outlet of the demister2The concentration is more than 100mg/m3And sampling and analyzing at the outlet of the supergravity reduction device, wherein the content of hydrogen peroxide in the dilute sulfuric acid product is 305 ppb.
Comparative example 14
As described in example 1, the hypergravity reduction apparatus was changed to an equivalent volume, isocatalyst-supported packed column without changing the other conditions.
Gas sample analysis, SO, at the gas outlet of the demister2The concentration is 28mg/m3And sampling and analyzing at the outlet of the supergravity reduction device, wherein the content of hydrogen peroxide in the dilute sulfuric acid product is 950 ppb.
Comparative example 15
As described in embodiment 1, the other conditions are not changed, and the liquid delivery pipeline behind the hydrogen peroxide flow regulating valve is changed from the liquid inlet pipeline connected with the supergravity absorbing device to the outlet pipeline connected with the supergravity absorbing device.
Sampling and analyzing at the gas outlet of the defoaming device, SO2The concentration is 30mg/m3And sampling and analyzing at the outlet of the supergravity reduction device, wherein the content of hydrogen peroxide in the dilute sulfuric acid product is 340 ppb.
The temperature of the cooled flue gas, the temperature and pressure in the supergravity absorption device, the supergravity level, the gas-liquid volume flow ratio and the concentration of dilute sulfuric acid during extraction influence the SO2The key factor of the removal effect. The temperature of the cooled flue gas is the same as the temperature in the supergravity absorption device, the temperature is too low, and hydrogen peroxide and SO are added2The reaction activity is reduced, the temperature is overhigh, and the decomposition rate of hydrogen peroxide is improved; the pressure in the supergravity absorption unit affects the SO2The higher the pressure is, the higher the solubility is, the more favorable the absorption is, but when the pressure is raised to a certain degree, the gas-liquid mass transfer efficiency is restricted by other degrees and is difficult to be continuously improved, and the requirement of maintaining high pressure on equipment is correspondingly improved; the higher the concentration of the hydrogen peroxide, the higher the concentration of the hydrogen peroxide and SO2The faster the reaction rate, the higher the concentration of residual hydrogen peroxide in the final product; the hypergravity level of the hypergravity absorption device is a key parameter of equipment, and is adjusted by changing the rotating speed of the hypergravity absorption equipment, the liquid phase can be broken into smaller infinitesimal elements when the rotating speed is higher, more surface area is exposed, the mass transfer efficiency is improved, but the liquid is thrown out more quickly due to the improvement of the rotating speed, and the gas-liquid contact time is shortened; the gas-liquid volume flow ratio is also the key to influence the absorption effect, the small gas-liquid ratio condition has better absorption effect, but the unit absorption liquid treated SO-containing2The smoke amount is small; accumulation of dilute sulfuric acid, as previously described, can result in a decrease in absorption, but to reduce the difficulty of dilute sulfuric acid purification, it is often desirable to obtain a dilute sulfuric acid product having a higher concentration; therefore, these process conditions need to be controlled in a proper range to obtain good SO with the lowest possible material energy consumption2Removal effect and dilute sulfuric acid product. For the decomposition of residual hydrogen peroxide in the produced dilute sulfuric acid, a supergravity technology is also adopted to strengthen the reduction process of the hydrogen peroxide, the catalyst load and the supergravity level of a supergravity reduction device are important parameters of the process, the catalyst load is too low, and liquid can leave without passing through a catalyst, so that the mass transfer efficiency is reduced, and under the condition of sufficient catalyst consumption, the decomposition of the hydrogen peroxide is limited by other factors; the effect of the supergravity level on the decomposition effect of hydrogen peroxide is similar to that on SO2The higher the level of supergravity, the higher the degree of liquid fragmentation, the larger the area of liquid contact with the catalyst, andon the one hand, the higher the level of hypergravity, the shorter the time for the liquid to contact the catalyst; therefore, the hydrogen peroxide decomposition process needs to control the load of the catalyst and the hypergravity level of the hypergravity reduction device.
In summary, to ensure SO2The removal effect, the quality of the dilute sulfuric acid product and the decomposition efficiency of the hydrogen peroxide are in good levels, the related process conditions should be controlled in a proper range, and if the conditions are not properly controlled, the process effect is reduced or the operation difficulty and the cost are increased.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.

Claims (1)

1. By using a gas containing SO2The method for preparing the dilute sulfuric acid by using the device for preparing the dilute sulfuric acid from the flue gas is characterized by comprising the following equipment: the device comprises a cooling and dedusting device (1), a supergravity absorption device (2), a defoaming device (3), a rich liquid storage tank (4), a rich liquid delivery pump (5), a rich liquid flow regulating valve (6), a dilute sulfuric acid flow regulating valve (7), a supergravity reduction device (8), a hydrogen peroxide storage tank (9), a hydrogen peroxide delivery pump (10) and a hydrogen peroxide flow regulating valve (11); wherein, the gas outlet of cooling dust collector (1) connects the gas inlet of hypergravity absorbing device (2), the gas outlet of hypergravity absorbing device (2) connects defoaming device (3), the liquid outlet of defoaming device (3) connects hypergravity absorbing device (2) liquid inlet pipeline, the liquid outlet of hydrogen peroxide solution storage tank (9) connects hypergravity absorbing device (2) liquid inlet pipeline through hydrogen peroxide solution delivery pump (10) and hydrogen peroxide solution flow control valve (11), the liquid outlet pipeline of hypergravity absorbing device (2) connects pregnant solution storage tank (4), the liquid outlet of pregnant solution storage tank (4) connects two branches through pregnant solution delivery pump (5), one connects hypergravity absorbing device (2) liquid inlet pipeline through pregnant solution flow control valve (6), one connects dilute sulphuric acid flow control valve (7) and hypergravity reduction device.(8) As a product extraction line;
the method comprises the following steps:
(1) containing SO2The flue gas enters a temperature-reducing and dust-removing device, the temperature is reduced, and solid impurities carried in the flue gas are removed;
(2) the gas cooled and dedusted in the step (1) enters a supergravity absorption device and contacts with absorbent hydrogen peroxide solution in the supergravity absorption device, and SO2Entering a liquid phase to form hydrogen peroxide mixed absorption liquid containing sulfuric acid, entering the desulfurized gas into a defoaming device to remove entrained absorption liquid, discharging the gas from a chimney or sending the gas to a downstream process, and returning the removed entrained absorption liquid to the supergravity absorption device;
(3) enabling the absorption rich solution subjected to desulfurization in the step (2) to enter a rich solution storage tank, circularly absorbing the rich solution in the rich solution storage tank through a rich solution delivery pump and a flow regulating valve, and extracting the rich solution through a dilute sulfuric acid flow regulating valve when the concentration of dilute sulfuric acid in the rich solution reaches a specified concentration;
(4) after the dilute sulfuric acid reaches the specified concentration in the step (3), extracting the dilute sulfuric acid by a dilute sulfuric acid flow regulating valve, feeding the dilute sulfuric acid into a supergravity reduction device, loading a hydrogen peroxide reduction catalyst on a filler used by the supergravity reduction device, removing residual hydrogen peroxide in the extracted dilute sulfuric acid under the action of the catalyst, and collecting or sending the dilute sulfuric acid to a downstream process as a product;
(5) hydrogen peroxide with a certain concentration is stored in the hydrogen peroxide storage tank, and when the concentration of hydrogen peroxide in the desulfurization absorption liquid is detected to be too low, the hydrogen peroxide can be supplemented in time through a hydrogen peroxide delivery pump and a hydrogen peroxide flow regulating valve;
wherein the temperature of the flue gas subjected to temperature reduction and dust removal in the step (1) is controlled to be 15-50 ℃; in the step (2), the pressure in the supergravity absorption device is 0.05-0.5 MPa, the temperature is 15-50 ℃, the initial concentration of the absorbent is 0.1-8 wt%, the supergravity level of the supergravity absorption device is 80-200, and the gas-liquid volume flow ratio in the supergravity absorption device is 200-650; the mass fraction of the dilute sulfuric acid product in the step (3) is 20-55 wt%; the filler used in the step (4) is loaded with a hydrogen peroxide reduction catalyst, the loading is 2-10 vol%, and the hypergravity level of the hypergravity reduction device is 90-180%; the reducing catalyst is selected from MnO2，CuO，Pt，Ag，Cr。
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