Strontium carbonate production waste gas and waste residue combined treatment system and process

Abstract

The invention relates to the technical field of chemical engineering, in particular to a strontium carbonate production waste gas and waste residue combined treatment system and technology.The strontium carbonate production waste gas and waste residue combined treatment system comprises a composite reaction tank, a clarification reaction kettle and a desulfurization tower, the vertical-flow reaction tank focuses on rapid sedimentation and primary treatment, the horizontal-flow sedimentation tank focuses on deep purification, the vertical-flow reaction tank and the horizontal-flow sedimentation tank are connected in series to form a multi-layer filtering system, calcium oxide in waste residues can be subjected to a curing reaction in the composite reaction tank, and meanwhile, calcium oxide reacts with sodium sulfite in the desulfurization tower to generate a sodium hydroxide solution; through the design of the system, the combined treatment of waste residues and waste gas is realized, the cost is reduced, and the efficiency is improved.

Description

Technical Field

[0001] The invention relates to the technical field of chemical industry, and in particular to a system and process for combined treatment of waste gas and waste residue from strontium carbonate production. Background Art

[0002] Strontium and strontium salts are widely used in the fields of electronics, chemical industry, metallurgy, military industry, functional materials and fireworks manufacturing. Celestine is the main strontium ore raw material for the production of various strontium salt compounds. A large amount of waste slag will be generated in the production process of strontium salts. Every 1t of strontium carbonate product will produce about 1.5t of waste slag. The main components of the waste slag are SiO2 and CaO. At the same time, waste gas will be generated in the production process of strontium salts, and the main component that needs to be removed in the waste gas is SO2 gas. Currently, the existing waste slag is usually used for building materials or landfill, and the waste gas is usually neutralized with NaOH solution or Ca(OH)2 slurry. The cost of using NaOH to treat waste gas is relatively high, especially in the industrial-grade waste gas treatment process, the waste gas treatment cost accounts for a large proportion, and the use of NaOH solution to treat waste gas increases the production cost of strontium carbonate. Therefore, industrial desulfurization usually uses Ca(OH)2 slurry to treat SO2 gas. Ca(OH)2 is slightly soluble in water. During the desulfurization process, Ca(OH)2 is usually made into slurry, and the waste gas is passed into the Ca(OH)2 slurry for desulfurization reaction. Since the particles of Ca(OH)2 slurry are large, it may cause pipeline blockage during transportation and use, affecting the normal operation of the system. In addition, calcium hydroxide is easily decomposed under alkaline conditions, resulting in the desulfurization effect of some waste gases failing to meet emission standards. Therefore, it is necessary to develop a treatment system that reduces costs and increases efficiency. Summary of the invention

[0003] The present invention aims to solve at least one of the technical problems existing in the prior art, and aims to reduce the production cost of strontium carbonate and improve the efficiency of sulfur dioxide treatment.

[0004] To this end, in a first aspect, the present invention provides a system for combined treatment of waste gas and waste residue from strontium carbonate production, comprising:

[0005] A composite reaction tank, wherein the composite reaction tank is provided with a vertical flow reaction tank and a horizontal flow sedimentation tank, the vertical flow reaction tank is provided with an outer cylinder, an overflow weir is provided at the upper end of the outer cylinder, and a collecting tank is provided around the overflow weir; the collecting tank is connected to the horizontal flow sedimentation tank;

[0006] A clarification reactor, wherein the clarification reactor is provided with an outer shell and an inner cylinder, wherein the upper end of the inner cylinder is fixedly connected to the top of the outer shell, and the lower end of the inner cylinder is open; the inner cylinder divides the outer shell into an inner clarification chamber and an outer sedimentation chamber; the sedimentation chamber and the advection sedimentation tank are connected through a first pipeline;

[0007] A desulfurization tower, wherein N annular baffles are arranged in a linear manner along the axial direction of the desulfurization tower, the annular baffles are inverted cone-shaped and have an opening at the center; an exhaust port is arranged at the upper end of the desulfurization tower; an air inlet pipe is arranged at the lower end of the desulfurization tower; the desulfurization tower is provided with a spray device, the spray device is provided with a spray main pipe and N spray branch pipes connected to the spray main pipe, each of the spray branch pipes is arranged below the annular baffle corresponding to the annular baffle, and the input end of the spray main pipe is connected to the clarification chamber through a second pipe; the lower part of the desulfurization tower is connected to the vertical flow reaction tank through a third pipe, wherein N≥2.

[0008] According to some embodiments of the present invention, the vertical flow reaction tank is provided with a crossbeam, and a center tube is provided on the crossbeam; the outer cylinder body is provided with a cylindrical portion and a conical cylinder portion in the vertical direction, the cylindrical portion is provided with a first clarification zone, and the conical cylinder portion is provided with a first sedimentation zone; the upper and lower ends of the center tube are respectively provided with openings, and a feeding zone is provided in the center tube; a reflector is provided below the center tube, and the reflector is located between the first clarification zone and the first sedimentation zone; a conical surface is provided at one end of the reflector plate close to the center tube, and the rotation center of the conical surface is colinear with the central axis of the center tube; one end of the third pipe passes through the outer cylinder body and the center tube in sequence, and the opening faces upward; a screen is provided above the third pipe in the center tube; a sludge extraction pipe is provided at the bottom of the conical cylinder portion; a centrifugal pump is provided on the sludge extraction pipe, and a diaphragm pump is provided on the third pipe.

[0009] According to some embodiments of the present invention, the horizontal flow sedimentation tank is provided with a second sedimentation zone and a second clarification zone along the horizontal direction; the bottom of the second clarification zone is provided with a slope; an overflow plate is slidably provided along the vertical direction between the horizontal flow sedimentation tank and the vertical flow reaction tank, and a serrated structure is provided on the overflow plate; adjustment devices are respectively provided on both sides of the overflow plate, and the adjustment devices include an adjustment base, a screw and a handwheel; the adjustment base is fixedly connected to the outer cylinder, the screw is threadedly connected to the adjustment base, the lower end of the screw is rotatably connected to the overflow plate, and the upper end of the screw is connected to the handwheel.

[0010] According to some embodiments of the present invention, the clarification reactor is provided with a scraper device; a funnel-shaped cylinder is provided at the lower end of the outer shell; the scraper device includes a rotary drive, a coupling, a control rod and a scraper, the rotary drive is fixedly connected to the upper end of the outer shell, the rotary drive is connected to the upper end of the control rod through a coupling, the lower end of the control rod passes through the outer shell and is detachably connected to the scraper; the contour line of the outer side of the scraper is parallel to the generatrix of the funnel-shaped cylinder; a first water pump is provided on the first pipeline, and a second water pump is provided on the second pipeline; the outer shell is provided with a mud discharge pipe at the lower end of the funnel-shaped cylinder, and a ball valve is provided on the mud discharge pipe.

[0011] According to some embodiments of the present invention, an hourglass-shaped structure is provided at the lower portion of the inner cylinder.

[0012] According to some embodiments of the present invention, a heat-insulating chamber is provided on the peripheral wall of the outer shell.

[0013] According to some embodiments of the present invention, the spray branch pipe includes a connecting pipe section and an annular pipe section, the axis of the connecting pipe section is horizontally arranged, one end of the connecting pipe section is connected to the spray main pipe, and the other end of the connecting pipe section is connected to the annular pipe section; an atomizing nozzle is arranged on the annular pipe section.

[0014] According to some embodiments of the present invention, the axis of the air inlet pipe is tangent to the inner circumferential wall of the desulfurization tower.

[0015] According to some embodiments of the present invention, a generatrix of the annular baffle and the axis have an angle β, wherein 45°≤β≤65°.

[0016] In a second aspect, the present application proposes a process for the combined treatment system of waste gas and waste residue from the production of strontium carbonate, comprising the following steps:

[0017] S01: putting sodium hydroxide particles or tablets into the advection sedimentation tank to prepare a sodium hydroxide circulating liquid; the pH value of the advection sedimentation tank is 10 to 13;

[0018] S02: inputting the sodium hydroxide circulating liquid into the clarification reactor for clarification;

[0019] S03: inputting the sodium hydroxide circulating liquid into the desulfurization tower, and atomizing the sodium hydroxide circulating liquid through the spraying device; at the same time, inputting the exhaust gas into the desulfurization tower for desulfurization reaction to generate a primary circulating liquid;

[0020] S04: putting the ground waste residue into the vertical flow reaction tank for aging reaction to generate calcium hydroxide slurry; the fineness of the waste residue is controlled to be 100 mesh to 250 mesh;

[0021] S05: inputting the primary circulating liquid into the vertical flow reaction tank; backwashing the waste residue, and at the same time, reacting the primary circulating liquid with the calcium hydroxide slurry to obtain a secondary circulating liquid;

[0022] S06: Clarifying the secondary circulation liquid in the vertical flow reaction tank;

[0023] S07: overflowing the secondary circulating liquid to the advection sedimentation tank to perform secondary clarification on the secondary circulating liquid; at the same time, adding sodium hydroxide granules or tablets to control the pH value of the advection sedimentation tank to be 10 to 13;

[0024] S08: inputting the secondary circulating liquid into the clarification reactor for tertiary clarification, wherein the ambient temperature in the clarification reactor is controlled to be 5°C to 40°C, and the retention time of the secondary circulating liquid in the clarification reactor is 0.5h to 1h;

[0025] S09: inputting the secondary circulating liquid into the desulfurization tower to react with the exhaust gas to obtain a tertiary circulating liquid;

[0026] S10: Loop steps S04 to S09.

[0027] A system and process for combined treatment of waste gas and waste residue from strontium carbonate production according to an embodiment of the present invention has at least the following beneficial effects:

[0028] According to the solution of the present invention, the combined treatment system of waste gas and waste residue from the production of strontium carbonate includes a composite reaction tank, a clarification reactor and a desulfurization tower, wherein the composite reaction tank is provided with a vertical flow reaction tank and a horizontal flow sedimentation tank, the vertical flow reaction tank focuses on rapid sedimentation and primary treatment, and the horizontal flow sedimentation tank focuses on deep purification, and the two are used in series to form a multi-level filtration system to ensure that the effluent water quality is more stable and reliable and meets the subsequent treatment standards. Compared with a single large-volume horizontal flow sedimentation tank, the vertical flow reaction tank occupies a smaller space and is suitable for situations where the site is limited. The design of the two in series not only saves land area, but also reduces construction and operation costs. The design of the vertical flow reaction tank and the horizontal flow sedimentation tank in series makes it easy to adjust parameters such as residence time and water flow rate according to the characteristics and treatment requirements of different waste residues and wastewaters, so that the entire system can maintain high-efficiency treatment performance.

[0029] According to the solution of the present invention, the outer cylinder is the basic frame of the composite reaction tank. The outer cylinder is usually designed to be cylindrical or square, and the material is mostly corrosion-resistant material to ensure long-term stable operation and resist erosion by various chemical media. An overflow weir is provided at the upper end of the outer cylinder to control the liquid level and maintain hydraulic balance. When the liquid in the vertical flow reaction tank rises above a predetermined height, the excess will flow out through the overflow weir and enter the collection tank surrounding it. The collection tank is arranged close to the horizontal flow sedimentation tank, and the horizontal flow sedimentation tank can receive overflow water from the vertical flow reaction tank through the collection tank. To ensure a smooth transition of the water flow and prevent turbulence. The collection tank is directly connected to the horizontal flow sedimentation tank through a pipeline or other appropriate diversion facilities, forming a seamless connection between the two units.

[0030] According to the solution of the present invention, the outer shell and the inner cylinder together constitute the main structure of the reactor. The upper end of the inner cylinder is tightly fixedly connected to the top of the outer shell to form a stable overall structure. The inner cylinder divides the outer shell into two independent but interconnected areas: the inner clarification chamber and the outer precipitation chamber. The layout of this structure effectively realizes the hierarchical separation and treatment of wastewater containing sodium hydroxide solution; when the wastewater containing sodium hydroxide solution first enters the precipitation chamber, the lighter clarified liquid will rise relatively still, while the heavier particles will fall under the influence of gravity, thereby realizing solid-liquid separation. The precipitated material is further deposited in the precipitation chamber, and the clarified liquid can be extracted through a specific outlet and enter the next processing link.

[0031] According to the solution of the present invention, multiple layers of annular baffles are arranged inside the desulfurization tower, and these baffles are evenly distributed along the axial direction of the tower body. The sulfur-containing exhaust gas passes through the desulfurization tower from bottom to top through the air inlet pipe, and meets the sodium hydroxide solution sprayed by the spray device in reverse. In this process, the sulfide in the gas reacts chemically with the sprayed sodium hydroxide solution, is absorbed or converted into a non-volatile form, and leaves the gas phase. The openings and inverted cone design on the annular baffles promote the gas to bypass, increase the contact opportunities between the gas and the scrubbing liquid, and improve the removal rate of harmful gases such as SO. As the exhaust gas continues to move upward, its pollution load is gradually reduced until it meets the emission standards when discharged from the top of the desulfurization tower. In addition, the bottom of the desulfurization tower is connected to the vertical flow reaction tank through a third pipeline to form a closed-loop flow, thereby improving the overall system efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 A structural schematic diagram of the present invention;

[0033] Figure 2 A schematic diagram of a planar structure of the present invention;

[0034] Figure 3 A schematic cross-sectional view of the present invention;

[0035] Figure 4 For the present invention Figure 3 A schematic diagram of the enlarged local structure at A;

[0036] Figure 5 It is a schematic diagram of the partial structure enlargement of the composite reaction pool of the present invention;

[0037] Figure 6 For the present invention Figure 3 A schematic diagram of the enlarged local structure at B;

[0038] Figure 7 It is a schematic diagram of the local structure of the bottom of the desulfurization tower of the present invention;

[0039] In the figure:

[0040] 100-composite reaction tank, 101-first clarification zone, 102-first sedimentation zone, 103-feeding zone, 104-second sedimentation zone, 105-second clarification zone, 110-vertical flow reaction tank, 111-outer cylinder, 112-overflow weir, 113-collecting tank, 114-center cylinder, 115-cylindrical part, 116-conical cylinder part, 117-reflecting plate, 118-screen, 120-adjustment sedimentation tank, 130-crossbeam, 140-overflow plate, 141-sawtooth structure, 160-adjusting device, 161-adjusting base, 162-screw, 163-hand wheel;

[0041] 200-clarification reaction kettle, 201-clarification chamber, 202-precipitation chamber, 210-outer shell, 211-funnel-shaped cylinder, 212-insulation chamber, 220-inner cylinder, 221-hourglass-shaped structure, 230-sludge scraping device, 231-rotation drive, 232-coupling, 233-control rod, 234-scraper, 240-sludge discharge pipe, 241-ball valve, 250-steel frame;

[0042] 300-desulfurization tower, 310-annular baffle, 320-exhaust port, 330-intake pipe, 340-spraying device, 341-spraying main pipe, 342-spraying branch pipe, 343-connecting pipe section, 353-annular pipe section, 360-atomizing nozzle, 370-working platform;

[0043] 400 - first pipeline, 410 - first water pump, 500 - second pipeline, 510 - second water pump, 600 - third pipeline, 610 - diaphragm pump, 700 - sludge extraction pipe, 710 - centrifugal pump. DETAILED DESCRIPTION

[0044] Embodiments of the present invention are described in detail below, examples of which are shown in the accompanying drawings, wherein the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain the present invention, and cannot be understood as limiting the present invention.

[0045] In the description of the present invention, it should be understood that descriptions involving orientation, such as orientation or positional relationship indicated as up, down, etc., are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0046] In the description of the present invention, "a plurality" means more than two. If there is a description of "first" or "second", it is only used for the purpose of distinguishing technical features, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features or implicitly indicating the order of the indicated technical features.

[0047] In the description of the present invention, unless otherwise clearly defined, terms such as setting, installing, connecting, etc. should be understood in a broad sense, and technicians in the relevant technical field can reasonably determine the specific meanings of the above terms in the present invention based on the specific content of the technical solution.

[0048] Reference Figures 1 to 7As shown, in the first aspect, the present invention discloses a combined treatment system for waste gas and waste residue from the production of strontium carbonate, comprising a composite reaction pool 100 , a clarification reactor 200 and a desulfurization tower 300 . Among them, the composite reaction tank 100 is provided with a vertical flow reaction tank 110 and a horizontal flow sedimentation tank 120, the vertical flow reaction tank 110 is provided with an outer cylinder 111, an overflow weir 112 is provided at the upper end of the outer cylinder 111, and a collecting tank 113 is provided on the peripheral side of the overflow weir 112; the collecting tank 113 is connected with the horizontal flow sedimentation tank 120; the clarification reactor 200 is provided with an outer shell 210 and an inner cylinder 220, the upper end of the inner cylinder 220 is fixedly connected to the top of the outer shell 210, and the lower end of the inner cylinder 220 is open; the inner cylinder 220 divides the outer shell 210 into an inner clarification chamber 201 and an outer sedimentation chamber 202; the sedimentation chamber 202 and the horizontal flow sedimentation tank 120 are connected through a first pipeline 400; N annular The baffle 310, N annular baffles 310 are linearly arranged along the axial direction of the desulfurization tower 300, the annular baffle 310 is an inverted cone structure and an opening is arranged at the central position; the upper end of the desulfurization tower 300 is provided with an exhaust port 320; the lower end of the desulfurization tower 300 is provided with an air inlet pipe 330; the desulfurization tower 300 is provided with a spray device 340, the spray device 340 is provided with a spray main pipe 341 and N spray branches 342 connected to the spray main pipe 341, each spray branch pipe 342 is arranged below the annular baffle 310 corresponding to the annular baffle 310, and the input end of the spray main pipe 341 is connected to the clarification chamber 201 through the second pipeline 500; the lower part of the desulfurization tower 300 is connected to the vertical flow reaction tank 110 through the third pipeline 600, wherein N≥2.

[0049] Reference Figure 1 As shown, in this embodiment, the number of composite reaction tanks 100, clarification reactors 200 and desulfurization towers 300 can be reasonably designed according to the treatment requirements of waste slag and waste gas. Specifically, in this embodiment, three groups of composite reaction tanks 100, two groups of clarification reactors 200, and two groups of desulfurization towers 300 are provided. In addition, the clarification reactor 200 is installed above the steel frame 250 to increase the gravitational potential energy of the solution in the clarification reactor 200. The solution is input into the desulfurization tower 300 in the clarification reaction tank, which can reduce energy consumption and increase pressure to meet the pressure requirements of atomization.

[0050] In this embodiment, the composite reaction tank 100 is provided with a vertical flow reaction tank 110 and a horizontal flow sedimentation tank 120. During operation, sodium hydroxide particles or tablets are first put into the horizontal flow sedimentation tank 120 to prepare a sodium hydroxide solution. The first batch of sodium hydroxide solution is used as a triggering agent, and will pass through the clarification reactor 200 and enter the desulfurization tower 300 for desulfurization reaction. The specific reaction formula is:

[0051] SO+2NaOH=NaSO+HO ①

[0052] NaSO is easily soluble in water, and the aqueous solution is alkaline. Sodium sulfite has reducing properties and can be oxidized to sodium sulfate by oxygen in the air. In addition, sodium sulfite also has bleaching and disinfecting effects.

[0053] At the same time, the staff puts the waste slag into the vertical flow reaction tank 110. Since the waste slag contains calcium oxide and other impurities, the calcium oxide in the waste slag undergoes a slaking reaction in the vertical flow reaction tank 110. The specific reaction formula is:

[0054] CaO+H2O=Ca(OH)2②

[0055] In the above reaction, calcium oxide absorbs moisture and reacts with water to form calcium hydroxide slurry. This process is usually accompanied by the release of heat.

[0056] At this time, the sodium sulfite solution generated by the desulfurization tower 300 is introduced into the vertical flow reaction tank 110 for precipitation reaction under certain conditions. The specific reaction formula is:

[0057] 2Na2SO3+2Ca(OH)2+O2→4NaOH+2CaSO4↓ ③

[0058] With the participation of oxygen, sodium sulfite and calcium hydroxide react, so when sodium sulfite solution is introduced, a certain amount of gas needs to be mixed in for reverse aeration treatment, and the NaOH solution generated by this reaction overflows into the horizontal flow sedimentation tank 120, thereby achieving the purpose of recycling. In this embodiment, since calcium hydroxide is slightly soluble in water and easily clogs pipes and nozzles, it can only be made into calcium hydroxide slurry for desulfurization treatment; and the cost of using sodium hydroxide solution alone for desulfurization reaction is relatively high. Therefore, the reaction mode of the structural design adopted, after the first input of sodium hydroxide, calcium hydroxide is prepared by adding waste residue, and new sodium hydroxide solution can be repeatedly produced for cyclic reaction, achieving the purpose of reducing costs and increasing efficiency.

[0059] Reference Figures 1 to 3As shown, in this embodiment, the combined treatment system of strontium carbonate production waste gas and waste residue includes a composite reaction tank 100, a clarification reactor 200 and a desulfurization tower 300, wherein the composite reaction tank 100 is provided with a vertical flow reaction tank 110 and a horizontal flow sedimentation tank 120, the vertical flow reaction tank 110 focuses on rapid sedimentation and primary treatment, and the horizontal flow sedimentation tank 120 focuses on deep purification, and the two are used in series to form a multi-level filtration system to ensure that the effluent water quality is more stable and reliable and meets the subsequent treatment standards. Compared with a single large-volume horizontal flow sedimentation tank 120, the vertical flow reaction tank 110 occupies a smaller space, which is suitable for limited sites. The design of the two in series not only saves land area, but also reduces construction and operation costs. The design of the vertical flow reaction tank 110 and the horizontal flow sedimentation tank 120 in series is adopted, and it is easy to adjust parameters such as residence time and water flow rate according to the characteristics and treatment requirements of different waste residues and wastewater, so that the whole system can maintain efficient treatment performance.

[0060] Reference Figures 3 to 5 As shown, in this embodiment, the outer cylinder 111 is the basic framework of the composite reaction tank 100. The design of the outer cylinder 111 is usually cylindrical or square, and the material is mostly corrosion-resistant material to ensure long-term stable operation and resist the erosion of various chemical media. An overflow weir 112 is provided at the upper end of the outer cylinder 111 to control the liquid level and maintain hydraulic balance. When the liquid in the vertical flow reaction tank 110 rises above a predetermined height, the excess part will flow out through the overflow weir 112 and enter the collection tank 113 surrounding its circumference. The collection tank 113 is arranged near the horizontal flow sedimentation tank 120, and the horizontal flow sedimentation tank 120 can receive overflow water from the vertical flow reaction tank 110 through the collection tank 113. To ensure a smooth transition of the water flow and prevent turbulence. The collection tank 113 is directly connected to the horizontal flow sedimentation tank 120 through a pipeline or other appropriate diversion facilities, forming a seamless connection between the two units.

[0061] Reference Figure 6 As shown, in this embodiment, the outer shell 210 and the inner cylinder 220 together constitute the main structure of the reactor. The upper end of the inner cylinder 220 is tightly fixedly connected to the top of the outer shell 210 to form a stable overall structure. The inner cylinder 220 divides the outer shell 210 into two independent but interconnected areas: the inner clarification chamber 201 and the outer precipitation chamber 202. The layout of this structure effectively realizes the hierarchical separation and treatment of wastewater containing sodium hydroxide solution; when the wastewater containing sodium hydroxide solution first enters the precipitation chamber 202, the lighter clarified liquid will rise relatively still, while the heavier particles will fall under the influence of gravity, thereby realizing solid-liquid separation. The precipitated material is further deposited in the precipitation chamber 202, and the clarified liquid can be extracted through a specific outlet and enter the next processing link.

[0062] Reference Figure 3 and Figure 7 As shown, in this embodiment, a plurality of annular baffles 310 are arranged inside the desulfurization tower 300, and these baffles are evenly distributed along the axial direction of the tower body. The sulfur-containing waste gas passes through the desulfurization tower 300 from bottom to top through the air inlet pipe 330, and meets the sodium hydroxide solution sprayed by the spray device 340 in reverse. In this process, the sulfide in the gas reacts chemically with the sprayed sodium hydroxide solution, is absorbed or converted into a non-volatile form, and leaves the gas phase. The opening and inverted cone design on the annular baffle 310 promote the gas to bypass, increase the contact opportunity between the gas and the scrubbing liquid, and improve the removal rate of harmful gases such as SO. As the waste gas continues to move upward, its pollution load is gradually reduced until it reaches the emission standard when discharged from the top of the desulfurization tower 300. In addition, the bottom of the desulfurization tower 300 is connected to the vertical flow reaction tank 110 through the third pipeline 600 to form a closed-loop flow, thereby improving the overall system efficiency.

[0063] In some embodiments of the present invention, the vertical flow reaction tank 110 is provided with a crossbeam 130, and a central cylinder 114 is provided on the crossbeam 130; the outer cylinder 111 is provided with a cylindrical portion 115 and a conical cylindrical portion 116 in the vertical direction, the cylindrical portion 115 is provided with a first clarification zone 101, and the conical cylindrical portion 116 is provided with a first precipitation zone 102; the central cylinder 114 is provided at the center of the cylindrical portion 115, and the upper and lower ends of the central cylinder 114 are respectively provided with openings, and a feeding zone 103 is provided in the central cylinder 114; a reflector 117 is provided below the central cylinder 114 to reflect The plate 117 is located between the first clarification zone 101 and the first sedimentation zone 102; a conical surface is provided at one end of the reflective plate 117 close to the central tube 114, and the center of rotation of the conical surface is collinear with the central axis of the central tube 114; one end of the third pipe 600 passes through the outer cylinder 111 and the central tube 114 in sequence, and the opening faces upward; a screen 118 is provided above the third pipe 600 in the central tube 114; a silt extraction pipe 700 is provided at the bottom of the conical cylinder 116; a centrifugal pump 710 is provided on the silt extraction pipe 700, and a diaphragm pump 610 is provided on the third pipe 600.

[0064] In this embodiment, the crossbeam 130 is erected above the outer cylinder 111, which is the supporting frame of the vertical flow reaction tank 110 and the transportation channel of the waste residue. The central cylinder 114 hoisted on the crossbeam 130 is at the geometric center of the vertical flow reaction tank 110, and constitutes the core component of the reaction tank. The central cylinder 114 runs through the upper and lower ends, and has the characteristics of opening at both ends. The feeding area 103 provided inside is the position where the waste residue and the treatment medium first contact. The outer cylinder 111 is designed as an upper cylindrical portion 115 and a lower conical cylinder portion 116. The cylindrical portion 115 is located in the first clarification area 101. Through the design of this structure, the first clarification area 101 and the feeding area 103 are relatively isolated, so as to avoid the reaction of calcium oxide and water in the waste residue to generate a large amount of heat to interfere with the clarification of sodium hydroxide in the first clarification area 101. This is mainly used to complete the preliminary solid-liquid mixing and reaction. The conical cylinder 116 is provided with the first precipitation area 102, which is conducive to the precipitation and concentration of larger particles. The reflector 117 is placed at the junction of the first clarification zone 101 and the first sedimentation zone 102. The design of its conical surface being colinear with the central axis of the central tube 114 cleverly guides the flow direction, causes the flow trajectory of the mixture to change, increases the sedimentation time of the mixture, and optimizes the reaction efficiency.

[0065] In this embodiment, the third pipeline 600 passes through the outer cylinder 111 and the central cylinder 114 in sequence to directly reach the feeding area 103, ensuring that the newly added wastewater can be accurately and unimpededly delivered to the feeding area 103. The screen 118 is arranged above the central cylinder 114 to receive the waste residue to prevent blockage of the subsequent process. At the same time, the opening of the third pipeline 600 is upward, and the waste residue on the screen 118 is backwashed and aerated. The sludge extraction pipe 700 at the bottom of the conical cylinder 116 cooperates with the centrifugal pump 710 to extract and remove the sediment. The diaphragm pump 610 equipped with the third pipeline 600 ensures the continuous supply and distribution of materials.

[0066] In some embodiments of the present invention, the horizontal flow sedimentation tank 120 is provided with a second sedimentation zone 104 and a second clarification zone 105 in the horizontal direction; the bottom of the second clarification zone 105 is provided with an inclined surface; an overflow plate 140 is slidably provided in the vertical direction between the horizontal flow sedimentation tank 120 and the vertical flow reaction tank 110, and a serrated structure 141 is provided on the overflow plate 140; adjustment devices 160 are respectively provided on both sides of the overflow plate 140, and the adjustment device 160 includes an adjustment base 161, a screw 162 and a handwheel 163; the adjustment base 161 is fixedly connected to the outer cylinder 111, the screw 162 is threadedly connected to the adjustment base 161, the lower end of the screw 162 is rotatably connected to the overflow plate 140, and the upper end of the screw 162 is connected to the handwheel 163.

[0067] In this embodiment, the overflow plate 140 is activated when the collection tank 113 is close to full load, and the excess water is released into the second sedimentation area 104 of the horizontal flow sedimentation tank 120 by opening the overflow, thereby avoiding the problem of water overflow or excessive pressure caused by overload of the collection tank 113, and maintaining the safe operation of the system. The adjustment device 160 allows the operator to adjust the position of the overflow plate 140 as needed, that is, to control the degree of opening and closing thereof in the vertical direction. In this way, the amount of water flowing into the horizontal flow sedimentation tank 120 can be adjusted in real time according to actual conditions, ensuring that the load of the downstream processing unit is moderate, avoiding the impact of a sudden increase in the amount of water, and maintaining the stability of the processing efficiency.

[0068] In this embodiment, the screw rod 162 can be driven in a variety of ways. Preferably, the screw rod 162 is driven by a hand wheel 163. The design of using the hand wheel 163 to drive the screw rod 162 reduces the processing cost and control cost of the system.

[0069] In this embodiment, a sawtooth structure 141 is provided at the upper end of the overflow plate 140. The sawtooth boundary structure can break the water surface tension and prevent foam and other light floating objects from overflowing with the water flow. These substances tend to easily block the overflow port, resulting in poor drainage. The presence of the sawtooth structure, especially its sharp edges and corners, can effectively cut or destroy the surface film, prevent foam accumulation, and reduce the risk of blockage. In addition, the sawtooth boundary helps to disperse the overflow water flow into multiple thin streams rather than a single thick flow, which not only reduces the impact force at a single point, but also forms a wider diffusion range in the horizontal flow sedimentation tank 120, which helps to evenly distribute the water flow, avoid local overload, and maintain stable operation of the system.

[0070] In some embodiments of the present invention, the clarification reactor 200 is provided with a scraper device 230; a funnel-shaped cylinder 211 is provided at the lower end of the outer shell 210; the scraper device 230 includes a rotary drive 231, a coupling 232, a control rod 233 and a scraper 234, the rotary drive 231 is fixedly connected to the upper end of the outer shell 210, the rotary drive 231 is transmission-connected to the upper end of the control rod 233 through the coupling 232, and the lower end of the control rod 233 passes through the outer shell 210 and is detachably connected to the scraper 234; the outer contour line of the scraper 234 is perpendicular to the generatrix of the funnel-shaped cylinder 211; a first water pump 410 is provided on the first pipeline 400, and a second water pump 510 is provided on the second pipeline 500; a mud discharge pipe 240 is provided at the lower end of the funnel-shaped cylinder 211 of the outer shell 210, and a ball valve 241 is provided on the mud discharge pipe 240.

[0071] Specifically, in this embodiment, the clarification reactor 200 includes an outer shell 210, an inner cylinder 220 and a scraper 230. The lower end of the inner cylinder 220 is open, and the inner cylinder 220 divides the outer shell 210 into a clarification chamber 201 and a sedimentation chamber 202; the outer cylinder 111 is the outer shell of the entire reactor, which not only provides physical support, but also plays a role in isolating the external environment. The inner cylinder 220 is placed inside the outer shell 210, and is closely connected to the top of the outer shell 210 at the top, and is open at the bottom to form an outlet. The design of this structure effectively divides the clarification chamber 201 and the sedimentation chamber 202 into two relatively independent spaces, avoiding fluid disturbance caused by the entry of external fluid, which interferes with the operation of the clarification chamber 201. When the liquid to be clarified enters the sedimentation chamber 202 through the first pipe 400, the heavier solid particles gradually sink to the bottom under the action of gravity. The inner cylinder 220 limits the flow path of the liquid to be clarified, so that the solid and liquid phases can be more fully separated in the clarification chamber 201. The clarified liquid is drawn out from the second pipe 500, while the sedimented material remains in the sedimentation chamber 202. In order to maintain the long-term efficient operation of the reactor, the sludge accumulated on the side wall of the outer shell 210 must be regularly removed. To this end, a rotatable scraper 234 is configured through the scraper device 230. These scrapers 234 can rotate and slide along the inner wall of the funnel-shaped cylinder 211, effectively remove the attachments on the inner wall of the funnel-shaped cylinder 211, prevent clogging, and ensure the internal cleanliness of the inner wall of the outer shell 210, thereby extending the service life.

[0072] Furthermore, a funnel-shaped cylinder 211 is provided at the lower end of the outer shell 210. In the present embodiment, the design of the funnel-shaped cylinder 211 increases the bottom slope angle of the outer shell 210, accelerates the sliding speed of solid particles, promotes rapid sedimentation, and effectively improves the separation efficiency. The inclined funnel wall makes it difficult for residual materials to be retained, reduces the possibility of bottom accumulation, facilitates regular cleaning, and makes maintenance work simple and quick. It can prevent sediment from silting up. Furthermore, the design of the funnel-shaped cylinder 211 forms a streamlined channel that helps the liquid to transition smoothly, avoids turbulence, protects the liquid in the clarification chamber from secondary contamination, and maintains a high-quality clarification effect.

[0073] Furthermore, the scraper device 230 includes a rotary drive 231, a coupling 232, a scraper 234 and a control rod 233. The rotary drive 231 is fixedly connected to the upper end of the outer shell 210, and the rotary drive 231 is connected to the upper end of the control rod 233 through the coupling 232. The lower end of the control rod 233 passes through the outer shell 210 and is detachably connected to the scraper 234. In this embodiment, the rotary drive 231 is installed at the upper end of the outer shell 210 as a power source to provide a stable rotation force for the scraper action. The coupling 232 can ensure the smoothness and efficiency of power transmission, connect the rotary drive 231 and the control rod 233, and ensure accurate docking during the energy conversion process. The upper end of the control rod 233 is tightly linked to the coupling 232, and the lower end of the control rod 233 extends to the inside of the reactor. Through the detachable connection with the scraper 234, the implementation and adjustment of the scraper action are realized. Through the design of this structure, the start and stop of the rotary drive 231 can be controlled by a preset program or manual command, and can be started as needed without human intervention, saving time and labor. The design of the length of the control rod 233 and the rotation radius of the scraper 234 can ensure that the scraper 234 touches all parts of the outer shell 210, leaving no dead corners, and completely removes dirt.

[0074] In some embodiments of the present invention, an hourglass-shaped structure 221 is provided at the lower part of the inner cylinder 220. The hourglass-shaped structure 221 is designed to guide the water flow to converge first and then slowly diffuse when moving upward, which can reduce the chance of the upper clear liquid being disturbed and improve the purity of the liquid in the clarification chamber.

[0075] In some embodiments of the present invention, a heat-insulating chamber 212 is provided on the peripheral wall of the outer shell 210. By providing the heat-insulating chamber 212 on the peripheral wall of the outer shell 210, antifreeze liquid can be injected into the heat-insulating chamber 212 when the ambient temperature is too low to prevent the liquid inside the outer shell 210 from freezing.

[0076] In some embodiments of the present invention, the spray branch pipe 342 includes a connecting pipe section 343 and an annular pipe section 353. The axis of the connecting pipe section 343 is horizontally arranged. One end of the connecting pipe section 343 is connected to the spray main pipe 341, and the other end of the connecting pipe section 343 is connected to the annular pipe section 353. An atomizing nozzle 360 ​​is arranged on the annular pipe section 353.

[0077] Specifically, in this embodiment, two groups of desulfurization towers 300 are provided, and a working platform 370 is provided on the upper part of the two groups of desulfurization towers 300. A plurality of annular baffles 310 are provided in the desulfurization tower 300, and the plurality of annular baffles 310 are linearly arranged along the axial direction of the desulfurization tower 300. The annular baffles 310 are in an inverted cone structure and an opening is provided at the central position; an exhaust port 320 is provided at the upper end of the desulfurization tower 300; an air inlet pipe 330 is provided at the lower end of the desulfurization tower 300; 0; The desulfurization tower 300 is provided with a spray device 340, and the spray device 340 is provided with a spray main pipe 341 and a plurality of spray branches 342 connected to the spray main pipe 341, each spray branch pipe 342 is respectively arranged below the annular baffle 310 corresponding to the annular baffle 310, and the input end of the spray main pipe 341 is connected to the clarification chamber 201 through the second pipeline 500; the lower part of the desulfurization tower 300 is connected to the vertical flow reaction tank 110 through the third pipeline 600. The spray branch pipe 342 includes a connecting pipe section 343 and an annular pipe section 353, the axis of the connecting pipe section 343 is arranged horizontally, one end of the connecting pipe section 343 is connected to the spray main pipe 341, and the other end of the connecting pipe section 343 is connected to the annular pipe section 353; an atomizing nozzle 360 ​​is arranged on the annular pipe section 353. During operation, when the exhaust gas containing SO enters the desulfurization tower 300 from the air inlet pipe 330 at the bottom of the desulfurization tower 300, it first passes through the annular baffle 310 at the bottom layer and meets the sodium hydroxide solution sprayed from the spray branch pipe 342 below. The SO in the exhaust gas dissolves in the sodium hydroxide solution and is absorbed through chemical reactions. As the exhaust gas continues to rise, it passes through each annular baffle 310 in turn, and each crossing is accompanied by the spraying of the sodium hydroxide solution until the purified gas is finally discharged from the top exhaust port 320. In this embodiment, through reasonable baffle design and precise spraying strategy, the desulfurization tower 300 can effectively improve the absorption efficiency of SO, reduce the pollutant content in the exhaust gas, and meet the requirements of environmental protection regulations. In addition, the design also helps to reduce energy consumption and operating costs, and improve the economy and sustainability of the entire system.

[0078] Furthermore, the design of the spray device 340 adopts a segmented structure, which is composed of a connecting pipe section 343 and an annular pipe section 353. The purpose of this design is to better adapt to the spatial structure and spraying requirements inside the desulfurization tower 300. Specifically, the main function of the connecting pipe section 343 is to serve as a bridge between the spray main pipe 341 and the annular pipe section 353, and is responsible for transmitting the sodium hydroxide solution from the main pipeline to the spray points of each layer. Its axis is set horizontally, ensuring that the sodium hydroxide solution can be smoothly and quickly transported to the designated location without being affected by gravity. One end of the connecting pipe section 343 is closely connected to the spray main pipe 341, and the other end is seamlessly connected to the annular pipe section 353 to form a complete liquid delivery channel. The annular pipe section 353 is laid around the periphery of the desulfurization tower 300, and it forms a closed ring along the edge of the annular baffle 310 for evenly distributing the alkaline liquid. Ensure that the alkaline liquid can evenly cover the entire area surrounded by the annular baffle 310 and the desulfurization tower 300, thereby improving the gas-liquid contact efficiency.

[0079] Furthermore, a plurality of atomizing nozzles 360 are arranged on the pipe wall of the annular pipe section 353, and all of the atomizing nozzles 360 are directed toward the central area of ​​the desulfurization tower 300; the atomizing nozzles 360 can convert the sodium hydroxide solution into mist-like fine particles; thereby providing a contact reaction between the alkaline liquid and the exhaust gas.

[0080] In some embodiments of the present invention, the axis of the air inlet pipe 330 is tangent to the inner circumferential wall of the desulfurization tower 300. Specifically, in the present embodiment, the axis of the air inlet pipe 330 is tangent to the inner circumferential wall of the desulfurization tower 300. Through the design of this structure. The exhaust gas can enter tangentially, and can generate a rotational motion tendency in the desulfurization tower 300, which helps the gas to be more evenly distributed in the space inside the desulfurization tower 300, especially in the bottom area of ​​the desulfurization tower 300. This increases the chance of gas-liquid contact in the initial stage and improves the initial desulfurization efficiency. The rotating airflow generated by the tangential inlet will excite strong vortices, accelerate the material transfer between the gas and liquid phases, especially for particles with higher density, which are more easily captured and settled, reducing the burden on the subsequent annular baffle 310. Compared with vertical entry, the tangential inlet design reduces the direct impact of the exhaust gas on the tower wall of the desulfurization tower 300, helps to reduce the wear and corrosion of the tower wall material, and also helps to prevent excessive accumulation of solid particles in a certain area and keep the tower unobstructed.

[0081] In some embodiments of the present invention, the generatrix and the axis of the annular baffle 310 have an angle β, wherein 45°≤β≤65°. Specifically, in the present embodiment, the generatrix and the axis of the annular baffle 310 have an angle β, wherein 45°≤β≤65°. Specifically, in the present embodiment, the angle β formed between the generatrix and the axis of the annular baffle 310 is set within the range of 45° to 65°, which is based on the optimization of gas-liquid contact efficiency and fluid mechanics. Through the design of this structure, the turbulence effect can be increased: when the exhaust gas passes through the annular baffle 310, the baffle arranged in a brim shape causes the airflow to produce a stronger turbulence effect when it hits the baffle. The contact area between the gas and the sodium hydroxide solution can be increased, thereby improving the absorption efficiency of harmful gases such as SO. The choice of angle directly affects the degree of change in the direction of the exhaust gas flow. The inclination angle of 45° to 65° balances the need to guide the smooth turning of the airflow and generate sufficient disturbance, which can effectively guide the exhaust gas to move upward along the tower body without causing excessive energy loss. Appropriate inclination design helps to spread the sodium hydroxide solution more evenly on the baffle surface, avoiding the occurrence of uneven distribution and ensuring that all areas can participate in the effective gas-liquid exchange reaction process.

[0082] In a second aspect, the present invention also provides a process for a system for combined treatment of waste gas and waste residue from strontium carbonate production, comprising the following steps:

[0083] S01: Put sodium hydroxide granules or tablets into the horizontal flow sedimentation tank 120 to prepare sodium hydroxide circulating liquid; the pH value of the horizontal flow sedimentation tank 120 is 10 to 13; before putting in, prepare the required sodium hydroxide granules or tablets to ensure that they meet the usage specifications and are not damp or deteriorated. Put sodium hydroxide into the horizontal flow sedimentation tank 120 according to the established proportion. This process should be done carefully to avoid splashing. After the addition is completed, continuously monitor the pH value and adjust the dosage to ensure that NaOH is fully dispersed and there is no local excessive concentration. Once the pH value of the circulating liquid is stable, it can be regarded as a preliminarily prepared sodium hydroxide circulating liquid, ready for use in subsequent processes.

[0084] S02: The sodium hydroxide circulating liquid is input into the clarification reactor 200 for clarification; since the initially prepared sodium hydroxide circulating liquid is relatively pure, no other treatment is performed when it passes through the clarification reactor 200 for the first time, and the circulation path is established.

[0085] S03: The sodium hydroxide circulating liquid is input into the desulfurization tower 300, and the sodium hydroxide circulating liquid is atomized through the spray device 340; at the same time, the waste gas is input into the desulfurization tower 300 for desulfurization reaction to generate a circulating liquid; when the prepared sodium hydroxide circulating liquid is sent to the desulfurization tower 300, it is first converted into a tiny droplet form through the spray device 340. This process greatly increases the contact area between the liquid and the gas, and promotes a more effective chemical reaction. The mist circulating liquid directly contacts the waste gas entering the desulfurization tower 300, and a substantial desulfurization reaction begins. The reaction generates a sodium sulfite solution.

[0086] S04: The ground waste residue is put into the vertical flow reaction tank 110 for slaking reaction to generate calcium hydroxide slurry; the fineness of the waste residue is controlled to be 100 mesh to 250 mesh; in this step, in order to ensure the reaction efficiency and product quality, the waste residue must be properly pretreated, that is, ground to a certain particle size requirement. Here, the target particle size is set between 100 mesh and 250 mesh. This fineness control, on the one hand, increases the specific surface area of ​​the waste residue and promotes the rapid progress of subsequent reactions, and on the other hand, it also helps to form a stable calcium hydroxide slurry.

[0087] S05: Input the primary circulating liquid into the vertical flow reaction tank 110; backwash the waste residue, and at the same time, the primary circulating liquid reacts with the calcium hydroxide slurry to obtain the secondary circulating liquid; in this step, the compacted waste residue can be removed by backwashing the waste residue. In this step, in order to further improve and promote the precipitation reaction, it is usually necessary to increase some gas in proportion when conveying the sodium sulfite solution, so that the waste residue is aerated, and finally a sodium hydroxide solution with certain impurities is produced.

[0088] S06: Clarify the secondary circulating liquid in the vertical flow reaction tank 110. In this step, clarifying the secondary circulating liquid is a key step to ensure the quality of wastewater treatment and improve the overall efficiency. This process is intended to further purify the secondary circulating liquid generated by various chemical reactions so as to better remove the residual suspended solids, colloidal particles and other possible impurities therein, thereby providing a purer fluid medium for the subsequent treatment stage.

[0089] S07: overflow the secondary circulating liquid to the advection sedimentation tank 120, and perform secondary clarification on the secondary circulating liquid; at the same time, add sodium hydroxide particles or tablets to control the pH value of the advection sedimentation tank 120 to 10 to 13; the secondary circulating liquid that has completed the first clarification will then overflow into the advection sedimentation tank 120. In this larger volume, the circulating liquid has more static time, so that smaller suspended matter and difficult-to-filter colloids have the opportunity to gradually settle down and undergo more in-depth clarification. In the advection sedimentation tank 120, sodium hydroxide NaOH particles or tablets will be added to adjust the pH value of the circulating liquid. The pH value is maintained between 10 and 13, which is a strong alkaline environment that is very conducive to the precipitation of metal ions and the decomposition of organic matter, helping to accelerate the precipitation process and improve treatment efficiency. At the same time, a high pH value also helps prevent the growth of harmful bacteria and ensure the safety and sanitation standards of the treatment process. Accurate control of pH is achieved through real-time monitoring and timely addition of sodium hydroxide. Instrument monitoring data guides the operator to decide when and how much NaOH should be added to maintain the desired target pH range. This dynamic regulation not only ensures the quality of wastewater treatment, but also saves on the use of chemicals and reduces operating costs.

[0090] S08: The secondary circulating liquid is input into the clarification reactor 200 for tertiary clarification. The ambient temperature in the clarification reactor 200 is controlled at 5°C to 40°C, and the residence time of the secondary circulating liquid in the clarification reactor 200 is 0.5h to 1h. In this step, the tertiary clarification stage is an important step for the final refining of the secondary circulating liquid. By performing deep treatment in the clarification reactor 200, it is ensured that the circulating liquid reaches a higher purity standard and is prepared for subsequent application or discharge. The environmental conditions inside the clarification reactor 200 are precisely set to optimize the clarification effect. The temperature is controlled between 5°C and 40°C, and this temperature range is considered to be most conducive to accelerating the precipitation process without introducing additional heat energy loss. At the same time, the residence time of the circulating liquid in the clarification reactor 200 is set at 0.5 hours to 1 hour, giving enough time for fine particles to complete precipitation, while also avoiding energy waste caused by staying for too long.

[0091] S09: The secondary circulating liquid is input into the desulfurization tower 300 to react with the exhaust gas to obtain a tertiary circulating liquid; in this step, the sodium hydroxide solution and the sulfur dioxide gas react again to generate a sodium sulfite solution.

[0092] S10: Circulate steps S04 to S09. By circulate steps S04 to S09, comprehensive treatment of waste residue and waste gas can be achieved.

[0093] Through the design of this process, the consumption of sodium hydroxide solution is significantly reduced by recycling the sodium hydroxide circulating liquid. At the same time, the comprehensive management of waste gas and waste residue is also realized, reflecting the concept of circular economy. By precisely controlling the reaction conditions, such as pH value, temperature, residence time, etc., the stability and efficiency of the process are ensured, and space is reserved for the expansion and upgrading of the system.

[0094] The embodiments of the present invention are described in detail above with reference to the accompanying drawings, but the present invention is not limited to the above embodiments, and various changes can be made within the knowledge scope of ordinary technicians in the relevant technical field without departing from the purpose of the present invention.

Claims

1. A combined treatment system for waste gas and waste residue from strontium carbonate production, characterized in that: include: A composite reaction tank (100), wherein the composite reaction tank (100) is provided with a vertical flow reaction tank (110) and a horizontal flow sedimentation tank (120), wherein the vertical flow reaction tank (110) is provided with an outer cylinder (111), an overflow weir (112) is provided at the upper end of the outer cylinder (111), and a collecting tank (113) is provided on the peripheral side of the overflow weir (112); the collecting tank (113) is connected to the horizontal flow sedimentation tank (120); A clarification reaction kettle (200), the clarification reaction kettle (200) being provided with an outer shell (210) and an inner cylinder (220), the upper end of the inner cylinder (220) being fixedly connected to the top of the outer shell (210), and the lower end of the inner cylinder (220) being open; the inner cylinder (220) dividing the outer shell (210) into an inner clarification chamber (201) and an outer sedimentation chamber (202); the sedimentation chamber (202) and the advection sedimentation tank (120) being connected via a first pipeline (400); A desulfurization tower (300), wherein N annular baffles (310) are arranged in the desulfurization tower (300), the N annular baffles (310) are linearly arranged along the axial direction of the desulfurization tower (300), the annular baffles (310) are in an inverted cone structure and are provided with an opening at a central position; an exhaust port (320) is provided at the upper end of the desulfurization tower (300); an air inlet pipe (330) is provided at the lower end of the desulfurization tower (300); the desulfurization tower (300) is provided with a spray device (340), the spray device (340) is provided with a spray main pipe (341) and N spray branch pipes (342) connected to the spray main pipe (341), each of the spray branch pipes (342) is respectively corresponding to the annular baffle (310) and is arranged below the annular baffle (310), the input end of the spray main pipe (341) is connected to the clarification chamber (201) through a second pipeline (500); the lower part of the desulfurization tower (300) is connected to the vertical flow reaction tank (110) through a third pipeline (600), wherein N≥2.

2. The combined treatment system for waste gas and waste residue from strontium carbonate production according to claim 1, characterized in that: The vertical flow reaction tank (110) is provided with a crossbeam (130), and a central cylinder (114) is provided on the crossbeam (130); the outer cylinder (111) is provided with a cylindrical portion (115) and a conical cylindrical portion (116) in the vertical direction, the cylindrical portion (115) is provided with a first clarification zone (101), and the conical cylindrical portion (116) is provided with a first sedimentation zone (102); the upper and lower ends of the central cylinder (114) are respectively opened, and a feeding zone (103) is provided in the central cylinder (114); a reflecting plate (117) is provided below the central cylinder (114), and the reflecting plate (117) is located between the first clarification zone (101) and the first sedimentation zone (102). The first sedimentation zone (102) is provided between the reflecting plate (117) and the central tube (114); a conical surface is provided at one end of the reflecting plate (117) close to the central tube (114), and the rotation center of the conical surface is colinear with the central axis of the central tube (114); one end of the third pipeline (600) passes through the outer cylinder (111) and the central tube (114) in sequence, and the opening faces upward; the central tube (114) is provided with a screen (118) above the third pipeline (600); a silt extraction pipe (700) is provided at the bottom of the conical cylinder (116); a centrifugal pump (710) is provided on the silt extraction pipe (700), and a diaphragm pump (610) is provided on the third pipeline (600).

3. The combined treatment system for waste gas and waste residue from strontium carbonate production according to claim 2, characterized in that: The horizontal flow sedimentation tank (120) is provided with a second sedimentation zone (104) and a second clarification zone (105); the bottom of the second clarification zone (105) is provided with an inclined surface; an overflow plate (140) is slidably provided in the vertical direction between the horizontal flow sedimentation tank (120) and the vertical flow reaction tank (110); the overflow plate (140) is provided with a sawtooth structure (141); the two sides of the overflow plate (140) are respectively provided with regulating The adjusting device (160) comprises an adjusting base (161), a screw rod (162) and a hand wheel (163); the adjusting base (161) is fixedly connected to the outer cylinder (111), the screw rod (162) is threadedly connected to the adjusting base (161), the lower end of the screw rod (162) is rotatably connected to the overflow plate (140), and the upper end of the screw rod (162) is connected to the hand wheel (163).

4. The combined treatment system for waste gas and waste residue from strontium carbonate production according to claim 1, characterized in that: The clarification reaction kettle (200) is provided with a scraper device (230); the lower end of the outer shell (210) is provided with a funnel-shaped cylinder (211); the scraper device (230) comprises a rotary drive (231), a coupling (232), a control rod (233) and a scraper (234); the rotary drive (231) is fixedly connected to the upper end of the outer shell (210); the rotary drive (231) is in transmission connection with the upper end of the control rod (233) through the coupling (232); the control rod (233) is in transmission connection with the upper end of the control rod (234); The lower end of the outer shell (210) and the scraper (234) are detachably connected; the outer contour line of the scraper (234) is parallel to the generatrix of the funnel-shaped cylinder (211); the first pipeline (400) is provided with a first water pump (410), and the second pipeline (500) is provided with a second water pump (510); the outer shell (210) is provided with a mud discharge pipe (240) at the lower end of the funnel-shaped cylinder (211), and the mud discharge pipe (240) is provided with a ball valve (241).

5. The system for combined treatment of waste gas and waste residue from strontium carbonate production according to claim 4, characterized in that: An hourglass-shaped structure (221) is provided at the lower portion of the inner cylinder (220).

6. The system for combined treatment of waste gas and waste residue from strontium carbonate production according to claim 5, characterized in that: A heat-insulating chamber (212) is provided on the peripheral wall of the outer shell (210).

7. The combined treatment system for waste gas and waste residue from strontium carbonate production according to claim 1, characterized in that: The spray branch pipe (342) comprises a connecting pipe section (343) and an annular pipe section (353); the axis of the connecting pipe section (343) is arranged horizontally; one end of the connecting pipe section (343) is connected to the spray main pipe (341), and the other end of the connecting pipe section (343) is connected to the annular pipe section (353); an atomizing nozzle (360) is arranged on the annular pipe section (353).

8. The combined treatment system for waste gas and waste residue from strontium carbonate production according to claim 7, characterized in that: The axis of the air inlet pipe (330) is tangent to the inner circumferential wall of the desulfurization tower (300).

9. The system for combined treatment of waste gas and waste residue from strontium carbonate production according to claim 7, characterized in that: The generatrix of the annular baffle (310) and the axis have an included angle β, wherein 45°≤β≤65°.

10. The process of the system for combined treatment of waste gas and waste residue from strontium carbonate production according to any one of claims 1 to 9, characterized in that: The following steps are involved: S01: putting sodium hydroxide particles or tablets into the advection sedimentation tank (120) to prepare a sodium hydroxide circulating liquid; the pH value of the advection sedimentation tank (120) is 10 to 13; S02: inputting the sodium hydroxide circulating liquid into the clarification reaction kettle (200) for clarification; S03: inputting the sodium hydroxide circulating liquid into the desulfurization tower (300), and atomizing the sodium hydroxide circulating liquid through the spraying device (340); at the same time, inputting the exhaust gas into the desulfurization tower (300) for desulfurization reaction to generate a primary circulating liquid; S04: putting the ground waste residue into the vertical flow reaction tank (110) to perform a slaking reaction to generate calcium hydroxide slurry; the fineness of the waste residue is controlled to be 100 mesh to 250 mesh; S05: inputting the primary circulating liquid into the vertical flow reaction tank (110); backwashing the waste residue, and reacting the primary circulating liquid with the calcium hydroxide slurry to obtain a secondary circulating liquid; S06: clarifying the secondary circulation liquid once in the vertical flow reaction tank (110); S07: overflowing the secondary circulation liquid to the horizontal flow sedimentation tank (120) to perform secondary clarification on the secondary circulation liquid; at the same time, adding sodium hydroxide granules or tablets to control the pH value of the horizontal flow sedimentation tank (120) to be 10 to 13; S08: inputting the secondary circulating liquid into the clarification reactor (200) for tertiary clarification, wherein the ambient temperature in the clarification reactor (200) is controlled to be 5°C to 40°C, and the retention time of the secondary circulating liquid in the clarification reactor (200) is 0.5h to 1h; S09: inputting the secondary circulating liquid into the desulfurization tower (300) to react with the waste gas for desulfurization to obtain a tertiary circulating liquid; S10: Loop steps S04 to S09.

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