Efficient treatment system and process capable of realizing simultaneous desulfurization, denitrification and decarbonization

Abstract

The invention discloses an efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization. The system comprises a supergravity reactor, an efficient gas-liquid rheological reactor, an absorption rich liquid buffer tank, an efficient liquid-liquid regeneration rheological reactor, a solid-liquid mixed liquid buffer tank, a solid-liquid separator and a regeneration absorption liquid buffer tank which are sequentially arranged. Aiming at the characteristics of tail gas in the high-energy-consumption industry, the invention develops an efficient flue gas treatment system and process capable of synchronously realizing desulfurization, denitrification and decarburization, a supergravity reactor, an efficient gas-liquid rheological reactor and an efficient liquid-liquid regeneration rheological reactor are adopted, and hydrogen peroxide and liquid caustic soda are selected as desulfurization, denitrification and decarburization reaction reagents; by using the alkaline industrial solid waste as the SO2 and CO2 curing raw material, high-efficiency, green and low-cost desulfurization, denitrification and decarburization can be realized, stable resource products can be generated, and regeneration and cyclic utilization of the liquid caustic soda can be realized.

Description

Technical Field

[0001] The present invention relates to the technical field of waste gas treatment, and in particular to a high-efficiency treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization. Background Art

[0002] In recent years, my country has stepped up its control over air pollutants from energy-intensive industries, resulting in a significant drop in emissions of sulfur dioxide and nitrogen oxides. However, the carbon dioxide content in exhaust gas from energy-intensive industries is high, resulting in large carbon emissions.

[0003] At present, the more mature desulfurization and denitrification treatment technology in high-energy-consuming industries is wet flue gas desulfurization (WFGD) + ammonia selective catalytic oxidation (NH3-SCR) technology, which can achieve simultaneous desulfurization and denitrification, but cannot decarbonize. In addition, this technology has the problem of deactivation of mainstream vanadium-titanium commercial SCR catalysts. At the same time, this technology has restricted the sulfur and nitrate control of flue gas in many high-energy-consuming industries due to its high investment and operating costs, catalyst replacement costs, and large land area. Therefore, in the face of the introduction of new environmental protection laws, new policies and other regulations, achieving simultaneous desulfurization, denitrification and decarbonization in high-energy-consuming industries has become the focus of industry attention, and it is urgent to develop efficient, green, and low-cost sulfur, nitrate and carbon coordinated purification technologies for tail gas characteristics of high-energy-consuming industries. Summary of the invention

[0004] The technical problem to be solved by the present invention is to provide an efficient treatment system and process that can achieve simultaneous desulfurization, denitrification and decarbonization in view of the deficiencies in the above-mentioned prior art.

[0005] In order to solve the above technical problems, the technical solution adopted by the present invention is: the first aspect of the present invention provides an efficient treatment system and process capable of realizing simultaneous desulfurization, denitrification and decarbonization, comprising an ultra-gravity reactor, an efficient gas-liquid rheological reactor, an absorption rich liquid buffer tank, an efficient liquid-liquid regeneration rheological reactor, a solid-liquid mixed liquid buffer tank, a solid-liquid separator and a regeneration absorption liquid buffer tank which are arranged in sequence;

[0006] The absorption rich liquid outlet of the high gravity reactor is connected to the absorption rich liquid inlet of the high efficiency gas-liquid rheological reactor, and the first flue gas outlet of the high gravity reactor is connected to the high efficiency gas-liquid rheological reactor;

[0007] The first liquid discharge port of the high-efficiency gas-liquid rheological reactor is connected to the absorption rich liquid buffer tank, and the absorption rich liquid buffer tank is simultaneously connected to the high-efficiency gas-liquid rheological reactor and the high-efficiency liquid-liquid regeneration rheological reactor;

[0008] The second liquid discharge port of the high-efficiency liquid-liquid regeneration rheological reactor is connected to a solid-liquid mixed liquid buffer tank, and the solid-liquid mixed liquid buffer tank is simultaneously connected to the high-efficiency liquid-liquid regeneration rheological reactor and the solid-liquid separator;

[0009] The solid-liquid separator is connected to the high-efficiency gas-liquid rheological reactor.

[0010] Preferably, the supergravity reactor further comprises a first absorption liquid inlet for adding absorption liquid and a first flue gas inlet for introducing flue gas to be treated, the first absorption liquid inlet is located at the top, and the first flue gas inlet is located at the bottom;

[0011] The high-efficiency gas-liquid rheological reactor comprises a gas-liquid rheological reactor body and a first ejector arranged on the upper part of the gas-liquid rheological reactor body;

[0012] The gas-liquid rheological reactor body is provided with an absorption rich liquid inlet, a first liquid discharge port, a second flue gas outlet and a regeneration liquid inlet;

[0013] The first ejector includes a first cylindrical pipe section, a first conical nozzle coaxially arranged in the first cylindrical pipe section, a first air inlet pipe tangentially connected to the first cylindrical pipe section, a first throat section connected to the first cylindrical pipe section, and a first diffusion pipe section connected to the first throat section.

[0014] Preferably, the high-efficiency liquid-liquid regeneration rheological reactor comprises a liquid-liquid regeneration rheological reactor body and a second ejector disposed on the upper portion of the liquid-liquid regeneration rheological reactor body;

[0015] The liquid-liquid regeneration rheological reactor body is provided with an industrial solid waste slurry inlet on the upper part and a second liquid discharge port on the lower part;

[0016] The second ejector includes a second cylindrical pipe section, a second conical nozzle coaxially arranged in the second cylindrical pipe section, a second air inlet pipe connected to the second cylindrical pipe section along a tangential direction, a lateral liquid inlet connected to the second cylindrical pipe section along a tangential direction, a second throat pipe section connected to the second cylindrical pipe section, and a second diffusion pipe section connected to the second throat pipe section, and the second air inlet pipe is connected to the external air environment.

[0017] Preferably, the absorption rich liquid outlet of the supergravity reactor is connected to the absorption rich liquid inlet of the gas-liquid rheological reactor body, and the first flue gas inlet is connected to the first air inlet pipe of the first ejector;

[0018] The first liquid discharge port of the high-efficiency gas-liquid rheological reactor is connected to the absorption rich liquid buffer tank, the outlet end of the absorption rich liquid buffer tank is connected to an absorption rich liquid circulation pump, and the outlet end of the absorption rich liquid circulation pump is simultaneously connected to the inlet end of the first conical nozzle of the first ejector and the lateral liquid inlet of the second ejector;

[0019] The second liquid discharge port of the high-efficiency liquid-liquid regeneration rheological reactor is connected to the solid-liquid mixed liquid buffer tank, the outlet end of the solid-liquid mixed liquid buffer tank is connected to a solid-liquid mixed liquid circulation pump, and the outlet end of the solid-liquid mixed liquid circulation pump is simultaneously connected to the inlet end of the second conical nozzle of the second ejector and the solid-liquid separator;

[0020] The solid-liquid separator is provided with a slag discharge port and a regeneration liquid outlet, and the regeneration liquid outlet is connected to the outlet end of the regeneration absorption liquid buffer tank and connected to the regeneration liquid inlet of the high-efficiency gas-liquid rheology reactor.

[0021] Preferably, both the absorption rich liquid buffer tank and the solid-liquid mixed liquid buffer tank are provided with vent pipes.

[0022] In a second aspect of the present invention, there is provided an efficient flue gas treatment process capable of simultaneously desulfurizing, denitrifying and decarbonizing, which uses the system as described above to treat the flue gas, and the process comprises the following steps:

[0023] S1, during the startup phase, a liquid alkali solution is pre-injected into the absorption rich liquid buffer tank, and an industrial solid waste slurry is injected into the high-efficiency liquid-liquid regeneration rheological reactor;

[0024] S2. The high-gravity reactor is turned on, and the flue gas to be treated is passed into the high-gravity reactor, and the hydrogen peroxide solution is passed into the high-gravity reactor to react with the incoming flue gas;

[0025] The flue gas treated by the supergravity reactor is discharged from the first ejector of the high-efficiency gas-liquid rheological reactor, and the No. 1 absorption rich liquid obtained after the reaction in the supergravity reactor is discharged from the first ejector of the high-efficiency gas-liquid rheological reactor;

[0026] S3, turning on the absorption rich liquid circulation pump, transporting part of the liquid in the absorption rich liquid temporary storage tank to the first ejector, mixing and reacting with the incoming flue gas in the first ejector, and then discharging into the gas-liquid rheological reactor body;

[0027] The No. 2 absorption rich liquid formed at the bottom of the gas-liquid rheological reactor body enters the absorption rich liquid temporary storage tank, and the treated flue gas is discharged from the high-efficiency gas-liquid rheological reactor;

[0028] Another part of the liquid in the absorption rich liquid temporary storage tank is transported by the absorption rich liquid circulation pump to the second ejector of the high-efficiency liquid-liquid regeneration rheological reactor;

[0029] S4, start the solid-liquid mixture circulation pump, transport the liquid in the solid-liquid mixture temporary storage tank to the second ejector, mix and react with the incoming air and No. 2 absorption rich liquid in the first ejector, and then discharge it into the regeneration rheological reactor body;

[0030] The solid-liquid mixture at the bottom of the regenerative rheological reactor body is discharged into the solid-liquid mixture temporary storage tank;

[0031] S5. Regularly monitor the Ca content in the solid-liquid mixed liquid in the solid-liquid mixed liquid temporary storage tank. 2+ Ion content, when Ca 2+ When the ion content is lower than the set value, the solid-liquid mixture is transported to the solid-liquid separator for solid-liquid separation, and the resulting supernatant enters the regeneration absorption liquid temporary storage tank, and then is transported to the high-efficiency gas-liquid rheology reactor through the regeneration liquid inlet for recycling.

[0032] Preferably, the efficient flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization comprises the following steps:

[0033] S1, during the startup phase, a liquid alkali solution is pre-injected into the absorption rich liquid buffer tank, and an industrial solid waste slurry is injected into the high-efficiency liquid-liquid regeneration rheological reactor;

[0034] S2, the high-gravity reactor is turned on, the flue gas to be treated is introduced into the high-gravity reactor from the first flue gas inlet, and the hydrogen peroxide solution is introduced into the high-gravity reactor from the first absorption liquid inlet to react with the incoming flue gas;

[0035] The flue gas treated by the ultra-gravity reactor is discharged from the first flue gas outlet and enters the high-efficiency gas-liquid rheological reactor through the first air inlet pipe. The No. 1 absorption rich liquid obtained after the reaction in the ultra-gravity reactor is discharged from the absorption rich liquid outlet and enters the said high-efficiency gas-liquid rheological reactor through the absorption rich liquid inlet.

[0036] S3, start the absorption rich liquid circulation pump, and transport part of the liquid in the absorption rich liquid temporary storage tank to the first conical nozzle of the first ejector, mix and react with the flue gas entering from the first air inlet pipe in the first ejector, and then discharge through the first diffuser section into the gas-liquid rheological reactor body;

[0037] The No. 2 absorption rich liquid formed at the bottom of the gas-liquid rheological reactor body is discharged from the first liquid discharge port into the absorption rich liquid temporary storage tank, and the treated flue gas is discharged from the high-efficiency gas-liquid rheological reactor from the second flue gas outlet;

[0038] Another part of the liquid in the absorption rich liquid temporary storage tank is transported by the absorption rich liquid circulation pump to the lateral liquid inlet on the second ejector of the high-efficiency liquid-liquid regeneration rheological reactor;

[0039] S4, start the solid-liquid mixed liquid circulation pump, transport the liquid in the solid-liquid mixed liquid temporary storage tank to the second conical nozzle of the second ejector, mix and react with the air entering from the second air inlet pipe and the No. 2 absorption rich liquid entering from the side liquid inlet in the first ejector, and then discharge through the second diffuser section into the regeneration rheological reactor body;

[0040] The solid-liquid mixed liquid at the bottom of the regenerative rheological reactor body is discharged from the second liquid discharge port into the solid-liquid mixed liquid temporary storage tank;

[0041] S5. Regularly monitor the Ca content in the solid-liquid mixed liquid in the solid-liquid mixed liquid temporary storage tank. 2+ Ion content, when Ca 2+ When the ion content is lower than the set value, the solid-liquid mixture is transported to the solid-liquid separator for solid-liquid separation, and the resulting supernatant enters the regeneration absorption liquid temporary storage tank, and then is transported to the high-efficiency gas-liquid rheology reactor through the regeneration liquid inlet for recycling.

[0042] Preferably, the mass concentration of the liquid alkali solution is 5% to 10%.

[0043] Preferably, the industrial solid waste slurry is prepared from calcium-containing industrial solid waste and water, with a liquid-to-solid ratio of 10 to 15 L / kg.

[0044] Preferably, the calcium-containing industrial solid waste is selected from at least one of steel slag, carbide slag, phosphogypsum and fly ash.

[0045] The beneficial effects of the present invention are:

[0046] Aiming at the characteristics of tail gas from high-energy-consuming industries, the present invention has developed a high-efficiency flue gas treatment system and process that can simultaneously achieve desulfurization, denitrification and decarbonization. The present invention adopts an ultra-gravity reactor, an high-efficiency gas-liquid rheological reactor, and an high-efficiency liquid-liquid regeneration rheological reactor, and selects hydrogen peroxide and liquid alkali as desulfurization, denitrification and decarbonization reaction reagents, and uses alkaline industrial solid waste (steel slag, fly ash, carbide slag, coal-fired fly ash, red mud, phosphogypsum, petroleum coke, steelmaking dust, etc.) as SO2 and CO2 solidification raw materials, which can achieve high-efficiency, green and low-cost desulfurization, denitrification and decarbonization, and can produce stable resource products, and can realize the regeneration and recycling of liquid alkali.

[0047] The present invention adopts an ultra-gravity reactor and two high-efficiency rheological reactors to achieve simultaneous desulfurization, denitrification and decarbonization of flue gas and sulfur and carbon fixation of industrial solid waste. The energy consumption of the whole process can be reduced by absorbing the rich liquid diversion. The absorption liquid can operate stably with high SO2 and CO2 absorption capacity, high circulation load and high regeneration efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] Figure 1 This is a schematic structural diagram of an efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization according to Example 1 of the present invention;

[0049] Figure 2 This is a schematic structural diagram of a high-efficiency gas-liquid rheological reactor according to Example 1 of the present invention;

[0050] Figure 3 This is a schematic structural diagram of a high-efficiency liquid-liquid regeneration rheological reactor according to Example 1 of the present invention.

[0051] Description of reference numerals:

[0052] 1—supergravity reactor; 11—first absorption liquid inlet; 12—first flue gas inlet; 13—absorption rich liquid outlet; 14—first flue gas outlet;

[0053] 2—high-efficiency gas-liquid rheological reactor; 21—gas-liquid rheological reactor body; 22—first ejector; 211—absorption rich liquid inlet; 212—regeneration liquid inlet; 213—second flue gas outlet; 214—first liquid discharge outlet; 221—first column pipe section; 222—first conical nozzle; 223—first air inlet pipe; 224—first throat pipe section; 225—first diffusion pipe section;

[0054] 3—absorption rich liquid buffer tank; 31—vent pipe;

[0055] 4—Absorption rich liquid circulation pump;

[0056] 5—high-efficiency liquid-liquid regeneration rheological reactor; 51—liquid-liquid regeneration rheological reactor body; 52—second ejector; 511—industrial solid waste slurry inlet; 512—second liquid discharge port; 521—second cylindrical pipe section; 522—second conical nozzle; 523—second air inlet pipe; 524—lateral liquid inlet; 525—second throat section; 526—second diffuser section;

[0057] 6—solid-liquid mixed liquid buffer tank; 61—vent pipe;

[0058] 7—solid-liquid mixed liquid circulation pump;

[0059] 8—solid-liquid separator; 81—regeneration liquid outlet; 82—slag discharge outlet;

[0060] 9—Regeneration absorption liquid buffer tank. DETAILED DESCRIPTION

[0061] The present invention is further described in detail below in conjunction with embodiments so that those skilled in the art can implement the invention with reference to the description.

[0062] It should be understood that the terms such as “having”, “including” and “comprising” used herein do not exclude the existence or addition of one or more other elements or combinations thereof.

[0063] The test methods used in the following examples are conventional methods unless otherwise specified. The materials and reagents used in the following examples are all commercially available unless otherwise specified. In the following examples, if no specific conditions are specified, the experiments were carried out under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used, if the manufacturer is not specified, are all conventional products that can be purchased commercially.

[0064] The present invention provides an efficient treatment system and process capable of achieving simultaneous desulfurization, denitration and decarbonization, comprising an ultra-gravity reactor 1, an efficient gas-liquid rheological reactor 2, an absorption rich liquid buffer tank 3, an efficient liquid-liquid regeneration rheological reactor, a solid-liquid mixed liquid buffer tank 6, a solid-liquid separator 8 and a regeneration absorption liquid buffer tank 9 which are sequentially arranged;

[0065] The absorption rich liquid outlet 13 of the high gravity reactor 1 is connected to the absorption rich liquid inlet 211 of the high efficiency gas-liquid rheological reactor 2, and the first flue gas outlet 14 of the high gravity reactor 1 is connected to the high efficiency gas-liquid rheological reactor 2;

[0066] The first liquid discharge port 214 of the high-efficiency gas-liquid rheological reactor 2 is connected to the absorption rich liquid buffer tank 3, and the absorption rich liquid buffer tank 3 is simultaneously connected to the high-efficiency gas-liquid rheological reactor 2 and the high-efficiency liquid-liquid regeneration rheological reactor;

[0067] The second liquid discharge port 512 of the high-efficiency liquid-liquid regeneration rheological reactor is connected to the solid-liquid mixed liquid buffer tank 6, and the solid-liquid mixed liquid buffer tank 6 is simultaneously connected to the high-efficiency liquid-liquid regeneration rheological reactor and the solid-liquid separator 8;

[0068] The solid-liquid separator 8 is connected to the high-efficiency gas-liquid rheological reactor 2 .

[0069] In the present invention, the supergravity reactor 1 also has a first absorption liquid inlet 11 for adding absorption liquid and a first flue gas inlet 12 for introducing flue gas to be treated. The first absorption liquid inlet 11 is located at the top, and the first flue gas inlet 12 is located at the bottom.

[0070] In the present invention, the high-efficiency gas-liquid rheological reactor 2 comprises a gas-liquid rheological reactor body 21 and a first ejector 22 disposed on the upper portion of the gas-liquid rheological reactor body 21;

[0071] The gas-liquid rheological reactor body 21 is provided with an absorption rich liquid inlet 211, a first liquid discharge port 214, a second flue gas outlet 213 and a regeneration liquid inlet 212;

[0072] The first ejector 22 includes a first cylindrical tube section 221, a first conical nozzle 222 coaxially arranged in the first cylindrical tube section 221, a first air inlet pipe 223 tangentially connected to the first cylindrical tube section 221, a first throat section 224 connected to the first cylindrical tube section 221, and a first diffuser section 225 connected to the first throat section 224. An air suction chamber is formed in the first cylindrical tube section 221 at the periphery of the first conical nozzle 222. The first conical nozzle 222 forms a jet to eject fluid, so that negative pressure is formed in the air suction chamber, so that suction can be generated in the first air inlet pipe 223 to inhale gas, and the gas and liquid are fully mixed inside, and the fluid is accelerated through the contracted first throat section 224, and then ejected from the first diffuser section 225, so as to achieve a gas-liquid efficient mixing reaction.

[0073] The flue gas treated in the high-efficiency gas-liquid rheological reactor 2 is finally discharged from the second flue gas outlet 213 .

[0074] In the present invention, the high-efficiency liquid-liquid regeneration rheological reactor comprises a liquid-liquid regeneration rheological reactor body 51 and a second ejector 52 disposed on the upper portion of the liquid-liquid regeneration rheological reactor body 51;

[0075] The upper part of the liquid-liquid regeneration rheological reactor body 51 is provided with an industrial solid waste slurry inlet 511, and the lower part is provided with a second liquid discharge port 512;

[0076] The second ejector 52 includes a second cylindrical tube section 521, a second conical nozzle 522 coaxially arranged in the second cylindrical tube section 521, a second air inlet pipe 523 tangentially connected to the second cylindrical tube section 521, a lateral liquid inlet 524 tangentially connected to the second cylindrical tube section 521, a second throat section 525 connected to the second cylindrical tube section 521, and a second diffuser section 526 connected to the second throat section 525. The second air inlet pipe 523 is connected to the external air environment. The working principle of the second ejector 52 is the same as that of the first ejector 22.

[0077] In the present invention, the absorption rich liquid outlet 13 of the supergravity reactor 1 is connected to the absorption rich liquid inlet 211 of the gas-liquid rheological reactor body 21, and the first flue gas inlet 12 is connected to the first air inlet pipe 223 of the first ejector 22;

[0078] The first liquid discharge port 214 of the high-efficiency gas-liquid rheological reactor 2 is connected to the absorption rich liquid buffer tank 3, and the outlet end of the absorption rich liquid buffer tank 3 is connected to the absorption rich liquid circulation pump 4. The outlet end of the absorption rich liquid circulation pump 4 is simultaneously connected to the inlet end of the first conical nozzle 222 of the first ejector 22 and the lateral liquid inlet 524 of the second ejector 52; the two routes are respectively controlled by setting valves for flow distribution.

[0079] The second liquid discharge port 512 of the high-efficiency liquid-liquid regeneration rheological reactor is connected to the solid-liquid mixed liquid buffer tank 6, and the outlet end of the solid-liquid mixed liquid buffer tank 6 is connected to the solid-liquid mixed liquid circulation pump 7. The outlet end of the solid-liquid mixed liquid circulation pump 7 is simultaneously connected to the inlet end of the second conical nozzle 522 of the second ejector 52 and the solid-liquid separator 8; the two routes are respectively controlled by setting valves for flow distribution.

[0080] The solid-liquid separator 8 is provided with a slag discharge port 82 and a regeneration liquid outlet 81 . The regeneration liquid outlet 81 is connected to the outlet end of the regeneration absorption liquid buffer tank 9 and connected to the regeneration liquid inlet 212 of the high-efficiency gas-liquid rheology reactor 2 .

[0081] In the present invention, both the absorption rich liquid buffer tank 3 and the solid-liquid mixed liquid buffer tank 6 are provided with vent pipes for discharging the internal air.

[0082] The present invention also provides a high-efficiency flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization, the process comprising the following steps:

[0083] S1, startup phase, pre-injecting liquid alkali solution into the absorption rich liquid buffer tank 3, and injecting industrial solid waste slurry into the high-efficiency liquid-liquid regeneration rheological reactor;

[0084] In a preferred embodiment, the mass concentration of the liquid caustic soda solution is 5% to 10%;

[0085] In a preferred embodiment, the industrial solid waste slurry is prepared from calcium-containing industrial solid waste and water, with a liquid-to-solid ratio of 10-15 L / kg. The calcium-containing industrial solid waste can be selected from at least one of high-calcium industrial solid wastes such as steel slag, carbide slag, phosphogypsum, fly ash, etc.

[0086] S2, the high-gravity reactor 1 is turned on, the flue gas to be treated is introduced into the high-gravity reactor 1 from the first flue gas inlet 12, and the hydrogen peroxide solution is introduced into the high-gravity reactor 1 from the first absorption liquid inlet 11 to react with the incoming flue gas;

[0087] The flue gas treated by the high gravity reactor 1 is discharged from the first flue gas outlet 14 and enters the high efficiency gas-liquid rheological reactor 2 through the first air inlet pipe 223. The No. 1 absorption rich liquid obtained after the reaction in the high gravity reactor 1 is discharged from the absorption rich liquid outlet 13 and enters the high efficiency gas-liquid rheological reactor 2 through the absorption rich liquid inlet 211.

[0088] The flue gas to be treated is waste gas containing sulfur, nitrogen and carbon dioxide. For example, in one embodiment, the flue gas composition is SO2 concentration ≤ 2000 mg / Nm 3 (dry state), NOx concentration ≤350mg / Nm 3 (dry state), NOx exists mainly in the form of NO, N2O4, NO2, CO2 concentration is 15% to 20%; the temperature is 100 to 150°C. The intake volume of flue gas is conventionally selected and adjusted according to the actual situation. For example, in one embodiment, the intake volume of flue gas is 100 to 200m 3 / h.

[0089] The flue gas inlet is led into the interior of the filler rotor of the supergravity reactor 1, and the hydrogen peroxide solution is pumped into the interior of the rotor by a liquid pump. Driven by the motor in the supergravity reactor 1, the filler rotor rotates at a high speed to form a supergravity field, so that the hydrogen peroxide solution is evenly sprayed onto the filler. When the flue gas is pumped into the filler, the flue gas and the hydrogen peroxide solution are in contact with a large area in the gaps of the filler and fully react. The flue gas after the reaction is discharged from the first flue gas outlet 14 above and enters the high-efficiency gas-liquid rheological reactor 2. The No. 1 absorption rich liquid after the reaction is evenly divided into droplets by the pores on the filler after high-speed rotation, and then directly thrown out of the periphery of the filler at a high speed to flow to the outer shell, and finally all flows to the absorption rich liquid outlet 13 for discharge, and enters the subsequent high-efficiency gas-liquid rheological reactor 2.

[0090] The main reactions occurring in the supergravity reactor 1 are:

[0091] N2O4+H2O2=2HNO3

[0092] 2NO2+H2O2=2HNO3

[0093] 2NO+3H2O2=2HNO3+2H2O

[0094] S3, start the absorption rich liquid circulation pump 4, and transport part of the liquid in the absorption rich liquid temporary storage tank to the first conical nozzle 222 of the first ejector 22, mix and react with the flue gas entering from the first air inlet pipe 223 in the first ejector 22, and then discharge through the first diffuser section 225 into the gas-liquid rheological reactor body 21;

[0095] The liquid in the absorption rich liquid temporary storage tank is ejected into a high-speed jet through the first conical nozzle 222, and a negative pressure is generated in the suction chamber around the jet outlet, and suction is generated at the first air inlet pipe 223 to suck the smoke into the first ejector 22; in the first ejector 22, the smoke is dispersed in the liquid in the form of small bubbles, and the gas-liquid two phases are fully mixed and contacted to form a high-speed foam vortex, the gas part is a strong turbulent flow, and the mass transfer efficiency is improved.

[0096] The No. 2 absorption rich liquid formed at the bottom of the gas-liquid rheological reactor body 21 is discharged from the first liquid discharge port 214 into the absorption rich liquid temporary storage tank, and the treated flue gas is discharged from the high-efficiency gas-liquid rheological reactor 2 from the second flue gas outlet 213;

[0097] Another part of the liquid in the absorption rich liquid temporary storage tank is transported by the absorption rich liquid circulation pump 4 to the lateral liquid inlet 524 on the second ejector 52 of the high-efficiency liquid-liquid regeneration rheological reactor;

[0098] The main reactions occurring in the high-efficiency gas-liquid reactor are as follows:

[0099] 2NaOH+SO2=Na2SO3+H2O

[0100] 2NaOH+CO2=Na2CO3+H2O

[0101] SO2+H2O2=H2SO4

[0102] 2NaOH+H2SO4=Na2SO4+2H2O

[0103] Na2SO3+H2O2=Na2SO4+H2O

[0104] NaOH+HNO3=NaNO3+H2O

[0105] S4, start the solid-liquid mixture circulation pump 7, transport the liquid in the solid-liquid mixture temporary storage tank to the second conical nozzle 522 of the second ejector 52, mix and react with the air entering from the second air inlet pipe 523 and the No. 2 absorption rich liquid entering from the lateral liquid inlet 524 in the first ejector 22, and then discharge through the second diffuser section 526 into the regenerative rheological reactor body;

[0106] The solid-liquid mixture at the bottom of the regenerative rheological reactor body is discharged from the second liquid discharge port 512 into the solid-liquid mixture temporary storage tank;

[0107] The liquid in the temporary storage tank of the solid-liquid mixture is ejected into a high-speed jet through the second conical nozzle 522, and the suction chamber around the jet outlet generates negative pressure, and part of the air is sucked into the second ejector 52 from the second air inlet pipe 523, and at the same time, the No. 2 absorption rich liquid entering from the lateral liquid inlet 524 is efficiently mixed with this part of the liquid and air, and the liquid-liquid two phases are fully mixed and contacted. Under the action of air, a high-speed foam vortex is formed, and the second ejector 52 is a strong turbulent flow, and the mass transfer efficiency is improved. The pH of the system is controlled by controlling the amount of liquid alkali added, and the pH of the system is maintained at 9.0-10.0. This process completes the regeneration of liquid alkali and the fixation of sulfur and carbon in industrial solid waste.

[0108] The main reactions occurring in the high-efficiency liquid-liquid regeneration reactor are as follows:

[0109] CaO+H2O=Ca(OH)2

[0110] Ca(OH)2+Na2CO3=CaCO3+2NaOH

[0111] Ca(OH)2+Na2SO4=CaSO4+2NaOH

[0112] S5. Regularly monitor the Ca content in the solid-liquid mixed liquid in the solid-liquid mixed liquid temporary storage tank. 2+ Ion content, when Ca 2+When the ion content is lower than the set value, the solid-liquid mixture is transported to the solid-liquid separator 8 for solid-liquid separation, and the resulting supernatant enters the regeneration absorption liquid temporary storage tank, and then is transported to the high-efficiency gas-liquid rheology reactor 2 through the regeneration liquid inlet 212 for recycling.

[0113] The above is the overall concept of the present invention, and detailed embodiments and comparative examples are provided below on the basis of the overall concept of the present invention to further illustrate the present invention.

[0114] Example 1

[0115] An efficient treatment system and process capable of achieving simultaneous desulfurization, denitration and decarbonization, comprising an ultra-gravity reactor 1, an efficient gas-liquid rheological reactor 2, an absorption rich liquid buffer tank 3, an efficient liquid-liquid regeneration rheological reactor, a solid-liquid mixed liquid buffer tank 6, a solid-liquid separator 8 and a regeneration absorption liquid buffer tank 9, which are arranged in sequence;

[0116] The absorption rich liquid outlet 13 of the high gravity reactor 1 is connected to the absorption rich liquid inlet 211 of the high efficiency gas-liquid rheological reactor 2, and the first flue gas outlet 14 of the high gravity reactor 1 is connected to the high efficiency gas-liquid rheological reactor 2;

[0117] The first liquid discharge port 214 of the high-efficiency gas-liquid rheological reactor 2 is connected to the absorption rich liquid buffer tank 3, and the absorption rich liquid buffer tank 3 is simultaneously connected to the high-efficiency gas-liquid rheological reactor 2 and the high-efficiency liquid-liquid regeneration rheological reactor;

[0118] The second liquid discharge port 512 of the high-efficiency liquid-liquid regeneration rheological reactor is connected to the solid-liquid mixed liquid buffer tank 6, and the solid-liquid mixed liquid buffer tank 6 is simultaneously connected to the high-efficiency liquid-liquid regeneration rheological reactor and the solid-liquid separator 8;

[0119] The solid-liquid separator 8 is connected to the high-efficiency gas-liquid rheological reactor 2 .

[0120] In this embodiment, the supergravity reactor 1 further comprises a first absorption liquid inlet 11 for adding absorption liquid and a first flue gas inlet 12 for introducing flue gas to be treated. The first absorption liquid inlet 11 is located at the top, and the first flue gas inlet 12 is located at the bottom.

[0121] In this embodiment, the high-efficiency gas-liquid rheological reactor 2 includes a gas-liquid rheological reactor body 21 and a first ejector 22 disposed on the upper portion of the gas-liquid rheological reactor body 21;

[0122] The gas-liquid rheological reactor body 21 is provided with an absorption rich liquid inlet 211, a first liquid discharge port 214, a second flue gas outlet 213 and a regeneration liquid inlet 212;

[0123] Among them, the first ejector 22 includes a first cylindrical pipe section 221, a first conical nozzle 222 coaxially arranged in the first cylindrical pipe section 221, a first air inlet pipe 223 tangentially connected to the first cylindrical pipe section 221, a first throat section 224 connected to the first cylindrical pipe section 221, and a first diffusion pipe section 225 connected to the first throat section 224.

[0124] The flue gas treated in the high-efficiency gas-liquid rheological reactor 2 is finally discharged from the second flue gas outlet 213 .

[0125] In this embodiment, the high-efficiency liquid-liquid regeneration rheological reactor comprises a liquid-liquid regeneration rheological reactor body 51 and a second ejector 52 disposed on the upper portion of the liquid-liquid regeneration rheological reactor body 51;

[0126] The upper part of the liquid-liquid regeneration rheological reactor body 51 is provided with an industrial solid waste slurry inlet 511, and the lower part is provided with a second liquid discharge port 512;

[0127] The second ejector 52 includes a second cylindrical tube section 521, a second conical nozzle 522 coaxially arranged in the second cylindrical tube section 521, a second air inlet pipe 523 tangentially connected to the second cylindrical tube section 521, a lateral liquid inlet 524 tangentially connected to the second cylindrical tube section 521, a second throat section 525 connected to the second cylindrical tube section 521, and a second diffuser section 526 connected to the second throat section 525. The second air inlet pipe 523 is connected to the external air environment. The working principle of the second ejector 52 is the same as that of the first ejector 22.

[0128] In this embodiment, the absorption rich liquid outlet 13 of the supergravity reactor 1 is connected to the absorption rich liquid inlet 211 of the gas-liquid rheological reactor body 21, and the first flue gas inlet 12 is connected to the first air inlet pipe 223 of the first ejector 22;

[0129] The first liquid discharge port 214 of the high-efficiency gas-liquid rheological reactor 2 is connected to the absorption rich liquid buffer tank 3, and the outlet end of the absorption rich liquid buffer tank 3 is connected to the absorption rich liquid circulation pump 4. The outlet end of the absorption rich liquid circulation pump 4 is simultaneously connected to the inlet end of the first conical nozzle 222 of the first ejector 22 and the lateral liquid inlet 524 of the second ejector 52; the two routes are respectively controlled by setting valves for flow distribution.

[0130] The second liquid discharge port 512 of the high-efficiency liquid-liquid regeneration rheological reactor is connected to the solid-liquid mixed liquid buffer tank 6, and the outlet end of the solid-liquid mixed liquid buffer tank 6 is connected to the solid-liquid mixed liquid circulation pump 7. The outlet end of the solid-liquid mixed liquid circulation pump 7 is simultaneously connected to the inlet end of the second conical nozzle 522 of the second ejector 52 and the solid-liquid separator 8; the two routes are respectively controlled by setting valves for flow distribution.

[0131] The solid-liquid separator 8 is provided with a slag discharge port 82 and a regeneration liquid outlet 81 . The regeneration liquid outlet 81 is connected to the outlet end of the regeneration absorption liquid buffer tank 9 and connected to the regeneration liquid inlet 212 of the high-efficiency gas-liquid rheology reactor 2 .

[0132] In this embodiment, a vent pipe 31 is provided on the absorption rich liquid buffer tank 3, and a vent pipe 61 is provided on the solid-liquid mixed liquid buffer tank 6, which are used to discharge the internal air.

[0133] This embodiment also provides a high-efficiency flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization, the process comprising the following steps:

[0134] S1, startup phase, pre-inject 80m3 of the absorption rich liquid buffer tank 3 3 Liquid alkali solution (sodium hydroxide solution), with a liquid concentration of 5% by weight, is injected into the industrial solid waste slurry in a high-efficiency liquid-liquid regeneration rheological reactor;

[0135] In this embodiment, the industrial solid waste slurry is prepared by mixing calcium-containing industrial solid waste with water, and the liquid-to-solid ratio is 10L / kg. The calcium-containing industrial solid waste is carbide slag grinding powder with a particle size of 200-250 mesh, and the main chemical components (in oxide form, mass ratio%) are: CaO 85.26%, SiO2 3.82%, Al2O3 0.94%, total iron 0.51%, and the rest are other impurities.

[0136] S2, the high-gravity reactor 1 is turned on, the flue gas to be treated is introduced into the high-gravity reactor 1 from the first flue gas inlet 12, and the hydrogen peroxide solution (with a concentration of 5 wt%) is introduced into the high-gravity reactor 1 from the first absorption liquid inlet 11 to react with the incoming flue gas;

[0137] The flue gas treated by the high gravity reactor 1 is discharged from the first flue gas outlet 14 and enters the high efficiency gas-liquid rheological reactor 2 through the first air inlet pipe 223. The No. 1 absorption rich liquid obtained after the reaction in the high gravity reactor 1 is discharged from the absorption rich liquid outlet 13 and enters the high efficiency gas-liquid rheological reactor 2 through the absorption rich liquid inlet 211.

[0138] In this embodiment, the composition of the flue gas to be treated is: SO2 concentration ≤ 2000 mg / Nm 3 (dry state), NOx concentration ≤350mg / Nm 3 (Dry state), NOx exists mainly in the form of NO, N2O4, NO2, CO2 volume concentration is 15% to 20%; the temperature fluctuates within the range of 100 to 150°C, and the flue gas intake volume is 150 to 180 m 3 / h range.

[0139] In this embodiment, the gas-liquid ratio is 50:1 (m 3 :kg) to control the flow rate of the hydrogen peroxide solution introduced into the supergravity reactor 1.

[0140] In this embodiment, the rotation speed of the ultra-gravity reactor 1 is controlled to fluctuate within the range of 700-800 rpm.

[0141] In this embodiment, the filler in the ultra-gravity reactor 1 is specifically a stainless steel wire mesh filler.

[0142] S3, start the absorption rich liquid circulation pump 4, and absorb part of the liquid in the rich liquid temporary storage tank (12m 3 / h flow rate) is transported to the first conical nozzle 222 of the first ejector 22, mixed with the flue gas entering from the first air inlet pipe 223 in the first ejector 22 for reaction, and then discharged through the first diffuser section 225 into the interior of the gas-liquid rheological reactor body 21;

[0143] The No. 2 absorption rich liquid formed at the bottom of the gas-liquid rheological reactor body 21 is discharged from the first liquid discharge port 214 into the absorption rich liquid temporary storage tank, and the treated flue gas is discharged from the high-efficiency gas-liquid rheological reactor 2 from the second flue gas outlet 213;

[0144] Absorb another part of the liquid in the rich liquid temporary storage tank (8m 3 / h flow rate) is transported by the absorbed rich liquid circulation pump 4 to the lateral liquid inlet 524 on the second ejector 52 of the high-efficiency liquid-liquid regeneration rheological reactor;

[0145] S4, start the solid-liquid mixture circulation pump 7, and transfer the liquid (12m 3 / h flow rate) is transported to the second conical nozzle 522 of the second ejector 52, mixed with the air entering from the second air inlet pipe 523 and the No. 2 absorption rich liquid entering from the side liquid inlet 524 in the first ejector 22 for reaction, and then discharged through the second diffuser section 526 into the interior of the regenerative rheological reactor body;

[0146] The solid-liquid mixture at the bottom of the regenerative rheological reactor body is discharged from the second liquid discharge port 512 into the solid-liquid mixture temporary storage tank;

[0147] A liquid alkali addition port is also provided on the side of the second column pipe section 521 of the second ejector 52 for adding liquid alkali to control the pH value of the system and maintain the pH value of the system in the second ejector 52 at 9.0-10.0. This process completes the regeneration of liquid alkali and the fixation of sulfur and carbon in industrial solid waste.

[0148] S5. Regularly monitor the Ca content in the solid-liquid mixed liquid in the solid-liquid mixed liquid temporary storage tank. 2+ Ion content, when Ca 2+When the ion content is lower than the set value (100 mg / L), the solid-liquid mixture is transported to the solid-liquid separator 8 for solid-liquid separation, and the resulting supernatant (regenerated absorption liquid) enters the regenerated absorption liquid temporary storage tank, and then is transported to the high-efficiency gas-liquid rheology reactor 2 through the regeneration liquid inlet 212 for recycling.

[0149] Flue gas treatment test:

[0150] The concentrations of SO2, NO, NO2, NOx and CO2 in the inlet and outlet flue gas of the high-efficiency gas-liquid rheological reactor 2 were determined by MH3200 ultraviolet flue gas analyzer; the sulfur and carbon contents (mass percentage %) in industrial solid waste raw materials and industrial solid waste carbon fixation products were determined by the American LECO CS-344 carbon-sulfur analyzer, and the industrial solid waste sulfur fixation rate (%) and carbon fixation rate (%) were calculated by the following formula:

[0151]

[0152] In the formula, m1 and m0 represent the mass of industrial solid waste carbon fixation products and industrial solid waste raw materials, s1 and s0 represent the sulfur content (mass percentage) in industrial solid waste carbon fixation products and industrial solid waste raw materials, c1 and c0 represent the carbon content (mass percentage) in industrial solid waste carbon fixation products and industrial solid waste raw materials.

[0153] The process of Example 1 was run continuously for one week, the absorption liquid was recycled for many times, and the SO2 concentration in the outlet flue gas was less than 30 mg / Nm 3 、NOx concentration<50mg / Nm 3 , CO2 concentration is less than 6%. After calculation, the average sulfur fixation rate is 0.26%, and the average carbon fixation rate is 56.2%. That is, the system can achieve simultaneous desulfurization, denitrification and decarbonization, and the liquid alkali can be recycled for many times, and resource products can be obtained at the same time.

[0154] Although the embodiments of the present invention have been disclosed as above, they are not limited to the applications listed in the specification and the implementation modes. They can be fully applied to various fields suitable for the present invention. For those familiar with the art, additional modifications can be easily implemented. Therefore, without departing from the general concept defined by the claims and the scope of equivalents, the present invention is not limited to specific details.

Claims

1. An efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization, characterized in that: It includes an ultra-gravity reactor, a high-efficiency gas-liquid rheological reactor, an absorption rich liquid buffer tank, a high-efficiency liquid-liquid regeneration rheological reactor, a solid-liquid mixed liquid buffer tank, a solid-liquid separator and a regeneration absorption liquid buffer tank which are arranged in sequence; The absorption rich liquid outlet of the high gravity reactor is connected to the absorption rich liquid inlet of the high efficiency gas-liquid rheological reactor, and the first flue gas outlet of the high gravity reactor is connected to the high efficiency gas-liquid rheological reactor; The first liquid discharge port of the high-efficiency gas-liquid rheological reactor is connected to the absorption rich liquid buffer tank, and the absorption rich liquid buffer tank is simultaneously connected to the high-efficiency gas-liquid rheological reactor and the high-efficiency liquid-liquid regeneration rheological reactor; The second liquid discharge port of the high-efficiency liquid-liquid regeneration rheological reactor is connected to a solid-liquid mixed liquid buffer tank, and the solid-liquid mixed liquid buffer tank is simultaneously connected to the high-efficiency liquid-liquid regeneration rheological reactor and the solid-liquid separator; The solid-liquid separator is connected to the high-efficiency gas-liquid rheological reactor.

2. The efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization according to claim 1, characterized in that: The supergravity reactor also has a first absorption liquid inlet for adding absorption liquid and a first flue gas inlet for introducing flue gas to be treated, the first absorption liquid inlet is located at the top, and the first flue gas inlet is located at the bottom; The high-efficiency gas-liquid rheological reactor comprises a gas-liquid rheological reactor body and a first ejector arranged on the upper part of the gas-liquid rheological reactor body; The gas-liquid rheological reactor body is provided with an absorption rich liquid inlet, a first liquid discharge port, a second flue gas outlet and a regeneration liquid inlet; The first ejector includes a first cylindrical pipe section, a first conical nozzle coaxially arranged in the first cylindrical pipe section, a first air inlet pipe tangentially connected to the first cylindrical pipe section, a first throat section connected to the first cylindrical pipe section, and a first diffusion pipe section connected to the first throat section.

3. The efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization according to claim 2, characterized in that: The high-efficiency liquid-liquid regeneration rheological reactor comprises a liquid-liquid regeneration rheological reactor body and a second ejector arranged on the upper part of the liquid-liquid regeneration rheological reactor body; The liquid-liquid regeneration rheological reactor body is provided with an industrial solid waste slurry inlet on the upper part and a second liquid discharge port on the lower part; The second ejector includes a second cylindrical pipe section, a second conical nozzle coaxially arranged in the second cylindrical pipe section, a second air inlet pipe connected to the second cylindrical pipe section along a tangential direction, a lateral liquid inlet connected to the second cylindrical pipe section along a tangential direction, a second throat pipe section connected to the second cylindrical pipe section, and a second diffusion pipe section connected to the second throat pipe section, and the second air inlet pipe is connected to the external air environment.

4. The efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization according to claim 3, characterized in that: The absorption rich liquid outlet of the supergravity reactor is connected to the absorption rich liquid inlet of the gas-liquid rheological reactor body, and the first flue gas inlet is connected to the first air inlet pipe of the first ejector; The first liquid discharge port of the high-efficiency gas-liquid rheological reactor is connected to the absorption rich liquid buffer tank, the outlet end of the absorption rich liquid buffer tank is connected to an absorption rich liquid circulation pump, and the outlet end of the absorption rich liquid circulation pump is simultaneously connected to the inlet end of the first conical nozzle of the first ejector and the lateral liquid inlet of the second ejector; The second liquid discharge port of the high-efficiency liquid-liquid regeneration rheological reactor is connected to the solid-liquid mixed liquid buffer tank, the outlet end of the solid-liquid mixed liquid buffer tank is connected to a solid-liquid mixed liquid circulation pump, and the outlet end of the solid-liquid mixed liquid circulation pump is simultaneously connected to the inlet end of the second conical nozzle of the second ejector and the solid-liquid separator; The solid-liquid separator is provided with a slag discharge port and a regeneration liquid outlet, and the regeneration liquid outlet is connected to the outlet end of the regeneration absorption liquid buffer tank and connected to the regeneration liquid inlet of the high-efficiency gas-liquid rheology reactor.

5. The efficient treatment system and process capable of achieving simultaneous desulfurization, denitrification and decarbonization according to claim 1, characterized in that: The absorption rich liquid buffer tank and the solid-liquid mixed liquid buffer tank are both provided with vent pipes.

6. An efficient flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization, characterized in that: The system according to any one of claims 1 to 5 is used to treat flue gas, and the process comprises the following steps: S1, during the startup phase, a liquid alkali solution is pre-injected into the absorption rich liquid buffer tank, and an industrial solid waste slurry is injected into the high-efficiency liquid-liquid regeneration rheological reactor; S2. The high-gravity reactor is turned on, and the flue gas to be treated is passed into the high-gravity reactor, and the hydrogen peroxide solution is passed into the high-gravity reactor to react with the incoming flue gas; The flue gas treated by the supergravity reactor is discharged from the first ejector of the high-efficiency gas-liquid rheological reactor, and the No. 1 absorption rich liquid obtained after the reaction in the supergravity reactor is discharged from the first ejector of the high-efficiency gas-liquid rheological reactor; S3, turning on the absorption rich liquid circulation pump, delivering part of the liquid in the absorption rich liquid buffer tank to the first ejector, mixing and reacting with the incoming flue gas in the first ejector, and then discharging into the gas-liquid rheological reactor body; The No. 2 absorption rich liquid formed at the bottom of the gas-liquid rheological reactor body enters the absorption rich liquid temporary storage tank, and the treated flue gas is discharged from the high-efficiency gas-liquid rheological reactor; Another part of the liquid in the absorption rich liquid temporary storage tank is transported by the absorption rich liquid circulation pump to the second ejector of the high-efficiency liquid-liquid regeneration rheological reactor; S4, start the solid-liquid mixture circulation pump, transport the liquid in the solid-liquid mixture temporary storage tank to the second ejector, mix and react with the incoming air and No. 2 absorption rich liquid in the first ejector, and then discharge it into the regeneration rheological reactor body; The solid-liquid mixture at the bottom of the regenerative rheological reactor body is discharged into the solid-liquid mixture temporary storage tank; S5. Regularly monitor the Ca content in the solid-liquid mixed liquid in the solid-liquid mixed liquid temporary storage tank. 2+ Ion content, when Ca 2+ When the ion content is lower than the set value, the solid-liquid mixture is transported to the solid-liquid separator for solid-liquid separation, and the resulting supernatant enters the regeneration absorption liquid temporary storage tank, and then is transported to the high-efficiency gas-liquid rheology reactor through the regeneration liquid inlet for recycling.

7. The high-efficiency flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization according to claim 6 is characterized in that: The process includes the following steps: S1, during the startup phase, a liquid alkali solution is pre-injected into the absorption rich liquid buffer tank, and an industrial solid waste slurry is injected into the high-efficiency liquid-liquid regeneration rheological reactor; S2, the high-gravity reactor is turned on, the flue gas to be treated is introduced into the high-gravity reactor from the first flue gas inlet, and the hydrogen peroxide solution is introduced into the high-gravity reactor from the first absorption liquid inlet to react with the incoming flue gas; The flue gas treated by the ultra-gravity reactor is discharged from the first flue gas outlet and enters the high-efficiency gas-liquid rheological reactor through the first air inlet pipe. The No. 1 absorption rich liquid obtained after the reaction in the ultra-gravity reactor is discharged from the absorption rich liquid outlet and enters the said high-efficiency gas-liquid rheological reactor through the absorption rich liquid inlet. S3, start the absorption rich liquid circulation pump, and transport part of the liquid in the absorption rich liquid temporary storage tank to the first conical nozzle of the first ejector, mix and react with the flue gas entering from the first air inlet pipe in the first ejector, and then discharge through the first diffuser section into the gas-liquid rheological reactor body; The No. 2 absorption rich liquid formed at the bottom of the gas-liquid rheological reactor body is discharged from the first liquid discharge port into the absorption rich liquid temporary storage tank, and the treated flue gas is discharged from the high-efficiency gas-liquid rheological reactor from the second flue gas outlet; Another part of the liquid in the absorption rich liquid temporary storage tank is transported by the absorption rich liquid circulation pump to the lateral liquid inlet on the second ejector of the high-efficiency liquid-liquid regeneration rheological reactor; S4, start the solid-liquid mixed liquid circulation pump, transport the liquid in the solid-liquid mixed liquid temporary storage tank to the second conical nozzle of the second ejector, mix and react with the air entering from the second air inlet pipe and the No. 2 absorption rich liquid entering from the side liquid inlet in the first ejector, and then discharge through the second diffuser section into the regeneration rheological reactor body; The solid-liquid mixed liquid at the bottom of the regenerative rheological reactor body is discharged from the second liquid discharge port into the solid-liquid mixed liquid temporary storage tank; S5. Regularly monitor the Ca content in the solid-liquid mixed liquid in the solid-liquid mixed liquid temporary storage tank. 2+ Ion content, when Ca 2+ When the ion content is lower than the set value, the solid-liquid mixture is transported to the solid-liquid separator for solid-liquid separation, and the resulting supernatant enters the regeneration absorption liquid temporary storage tank, and then is transported to the high-efficiency gas-liquid rheology reactor through the regeneration liquid inlet for recycling.

8. The high-efficiency flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization according to claim 6 is characterized in that: The mass concentration of the liquid alkali solution is 5% to 10%.

9. The high-efficiency flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization according to claim 6 is characterized in that: The industrial solid waste slurry is prepared by mixing calcium-containing industrial solid waste with water, and the liquid-to-solid ratio is 10-15L / kg.

10. The high-efficiency flue gas treatment process capable of simultaneous desulfurization, denitrification and decarbonization according to claim 9, characterized in that: The calcium-containing industrial solid waste is selected from at least one of steel slag, carbide slag, phosphogypsum and fly ash.

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