A method and apparatus for treating sulfur-containing waste gas and waste liquid

Abstract

The application discloses a kind of sulfur-containing waste gas, waste liquid processing method and equipment, more particularly to sulfur-containing waste gas, waste liquid processing technical field, a kind of sulfur-containing waste gas, waste liquid processing method, characterized in that, the method includes: pyrolysis incineration unit, catalytic oxidation unit, condensation enrichment unit, tail gas purification unit, by sulfur-containing waste gas, waste liquid sequentially through pyrolysis incineration is sulfur dioxide, then converted into sulfur trioxide, and condensation forms sulfuric acid, then in the conversion of sulfur dioxide in tail gas, and is washed by water to form dilute acid, after that, under the action of high-voltage electric field, remove sulfur trioxide acid mist in tail gas, and discharge from chimney, under the ultra-clean emission of tail gas emission index and reach the effect of total sulfur high recovery rate.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of treatment of sulfur-containing waste gas and waste liquid, in particular to a treatment method and device for sulfur-containing waste gas and waste liquid. BACKGROUND

[0002] The current treatment of sulfur-containing waste gas mainly includes physical method, chemical method and biological method. The physical method includes adsorption method and condensation method. Although the equipment of the two methods is simple, the treatment efficiency is low, the operation cost is high, and secondary pollution is easy to cause. The chemical method mainly includes absorption method and catalytic combustion method. The absorption method has the disadvantages of high investment cost and high operation cost, and may produce a large amount of secondary pollution waste; the catalytic combustion method has high operation cost and high requirement for the pretreatment of waste gas. The biological method is limited by region, season, operation condition and the like, and has low purification efficiency.

[0003] The current disposal technology of sulfur-containing waste liquid includes acid recovery method, precipitation method, biochemical treatment method and oxidation method. The acid recovery method has high requirement for the sealing property and corrosion resistance of equipment, high investment and poor popularization; the precipitation method has poor precipitation property and high treatment cost; the biochemical treatment method has high requirement for the water quality of waste liquid, long treatment time and easy impact on microorganisms; the oxidation method includes direct oxidation and catalytic oxidation. The direct oxidation is suitable for occasions with small amount of sulfur, and has the disadvantages of high treatment cost and safety risk of oxidizing agent; the catalytic oxidation is suitable for high-concentration sulfur-containing waste water, and has high requirement for reaction conditions and needs to continuously add catalyst. Therefore, the present application provides a treatment method and device for sulfur-containing waste gas and waste liquid to solve the above problems. SUMMARY

[0004] The present application aims to provide a treatment method and device for sulfur-containing waste gas and waste liquid to solve the problems in the background art.

[0005] To achieve the above-mentioned purpose, the present application provides the following technical scheme: a treatment method for sulfur-containing waste gas and waste liquid, characterized in that the method comprises:

[0006] A pyrolysis incineration unit, which comprises a pyrolysis incineration furnace and a waste heat recovery furnace:

[0007] The sulfur-containing waste gas and waste liquid are added to the inside of the pyrolysis incineration furnace, fuel gas and combustion air are injected into the inside of the pyrolysis incineration furnace, the sulfur-containing waste gas and waste liquid are pyrolysis incinerated to generate high-temperature steam containing sulfur dioxide, and the high-temperature steam containing sulfur dioxide is cooled and heat energy is recovered through the waste heat recovery furnace;

[0008] A catalytic oxidation unit, which comprises a segmented sulfur dioxide reactor using a PTIL-WXP series catalyst:

[0009] The high-temperature steam containing sulfur dioxide enters the sectional sulfur dioxide reactor, and the sulfur dioxide is oxidized into sulfur trioxide;

[0010] The condensing concentration unit comprises a sulfuric acid condensate collection tank, a condenser, a sulfuric acid cooler, and a sulfuric acid storage tank:

[0011] The sulfur trioxide process gas is condensed into liquid sulfuric acid in the condenser when exchanging heat with the air taken from the environment, and flows into the sulfuric acid condensate collection tank under the action of gravity, and is stored in the sulfuric acid storage tank after being cooled by the sulfuric acid cooler;

[0012] The tail gas purification unit comprises a PTIL-CC reactor, a high-efficiency mist eliminator, and a chimney:

[0013] The process gas from the top of the condenser enters the PTIL-CC reactor, the residual sulfur dioxide gas in the PTIL-CC reactor is oxidized into sulfur trioxide, and the sulfur trioxide is washed by water in the PTIL-CC reactor to become dilute acid, and finally flows into the sulfuric acid storage tank, and the process gas enters the high-efficiency mist eliminator, and the sulfur dioxide acid mist in the tail gas is removed under the action of a high-voltage electric field, and is discharged from the chimney.

[0014] Preferably, the temperature of the cracking incineration is controlled at 950-1050℃, and the pressure in the cracking incinerator is controlled at -1-0KPa micro-negative pressure.

[0015] Preferably, the outlet of the sectional sulfur dioxide reactor is provided with a plate heat exchanger, the plate heat exchanger uses high-pressure saturated steam / high-pressure saturated steam water to exchange heat with the process gas to take away the reaction heat, the temperature of the inlet of the sectional sulfur dioxide reactor is controlled at 380-420℃, the temperature of the outlet of the catalytic oxidation unit is controlled at 270-290℃, and the pressure is controlled at 0-1KPa micro-positive pressure.

[0016] Preferably, the process gas side of the condenser is maintained at -1-0KPa micro-negative pressure, and the outlet temperature of the condenser is controlled at 90-110℃.

[0017] Preferably, the device comprises a cracking incinerator, a waste heat recovery furnace, a sectional sulfur dioxide reactor, a sulfuric acid condensate collection tank, a condenser, a PTIL-CC reactor, a high-efficiency mist eliminator, a chimney, a sulfuric acid cooler, a sulfuric acid storage tank, and a device mounting support;

[0018] The cracking incinerator, the waste heat recovery furnace, the sectional sulfur dioxide reactor, the sulfuric acid condensate collection tank, the condenser, the PTIL-CC reactor, the high-efficiency mist eliminator, the chimney, the sulfuric acid cooler, and the sulfuric acid storage tank are all mounted above the device mounting support, and the top of the cracking incinerator is provided with a feeding pipe and gas inlets for fuel gas and combustion air;

[0019] The top of the outer surface of the cracking incinerator is provided with a guide heat dissipation pipe for discharging process gas.

[0020] The top of the outer surface of the cracking incinerator is provided with a guide heat dissipation pipe for discharging process gas.

[0021] Preferably, the waste heat recovery furnace comprises a waste heat recovery furnace body, an outer layer cavity, an inner cavity, and a guide cyclone vane.

[0022] A cylindrical partition is arranged in the middle of the waste heat recovery furnace body, which separates the inside of the cracking incinerator into an outer layer cavity and an inner cavity.

[0023] The guide heat dissipation pipe comprises a main pipe and a branch pipe, the branch pipe is connected to the main pipe, and the branch pipe is arranged in the outer layer cavity.

[0024] Preferably, the segmented sulfur dioxide reactor comprises a first reaction tank body, a catalyst bed layer, a shunt layer plate, a self-adaptive upper frame, a spring, and a detachable pull-out frame.

[0025] The inside of the first reaction tank body is vertically provided with a mounting groove matched with the catalyst bed layer, the shunt layer plate, and the outer frame of the self-adaptive upper frame.

[0026] The middle part of the shunt layer plate is in an arc structure gradually downward from the middle to the outside, and the middle part of the shunt layer plate is provided with a ventilation hole.

[0027] The catalyst bed layer and the shunt layer plate are arranged alternately, the self-adaptive upper frame is arranged at the bottom, and the bottom of the self-adaptive upper frame is connected with the spring, and the bottom end of the spring is arranged at the bottom of the mounting groove.

[0028] Preferably, the condenser comprises a condenser body and a glass condensing tube.

[0029] The glass condensing tube is arranged in the inside of the condenser body, and the glass condensing tube is in a spiral shape.

[0030] Preferably, the PTIL-CC reactor comprises a second reaction tank body, a water spraying pipe, a catalyst bed layer, and a cylindrical barrel.

[0031] The middle of the top of the second reaction tank body is provided with a cylinder, and the cylinder is communicated with the gas outlet, the bottom end of the cylinder is in a suspended state, and the catalytic bed is installed between the inner wall of the second reaction tank body and the outer wall of the cylinder,

[0032] The top end of the inner wall of the cylinder is provided with a water injection pipeline.

[0033] Compared with the prior art, the beneficial effects of the present application are that:

[0034] 1. By treating the sulfur-containing waste gas and waste liquid through the pyrolysis incineration unit, the catalytic oxidation unit, the condensation concentration unit and the tail gas purification unit in sequence, the sulfur dioxide gas can be converted into sulfur trioxide gas, and the sulfur trioxide gas is hydrated to form sulfuric acid vapor and is condensed to produce finished sulfuric acid. At the same time, sulfuric acid can be produced from the sulfur dioxide in the condensed tail gas under the action of a low-temperature active catalyst, and acid mist is removed in a high-efficiency demister. The tail gas emission meets the emission index, and the total sulfur recovery rate is high.

[0035] 2. By cooperating the self-adaptive top frame and the spring, the number of catalyst bed layers can be changed according to the specific use condition under the action of the installation and dismounting pull-out frame, so that the catalyst bed layers can be conveniently used and replaced through the pull-out mode of the installation and dismounting pull-out frame, thereby facilitating the use. BRIEF DESCRIPTION OF DRAWINGS

[0036] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings needed to be used in the embodiments or the prior art description will be briefly introduced. Obviously, the drawings in the following description are only some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative labor.

[0037] Figure 1 It is a flowchart of the present application.

[0038] Figure 2 It is a structural schematic diagram of the present application.

[0039] Figure 3 It is a structural schematic diagram of the present application in front view.

[0040] Figure 4 It is a structural schematic diagram of the present application in cross-section view.

[0041] Figure 5 It is a structural schematic diagram of the present application in front view.

[0042] Figure 6 It is a structural schematic diagram of the present application in front view.

[0043] Figure 7 Figure 1 is a structural schematic diagram of a glass condenser tube in the present application.

[0044] Figure 8 Figure 2 is a structural schematic diagram of an adaptive upper top frame in the present application.

[0045] Figure 1 is a structural schematic diagram of a glass condenser tube in the present application. DETAILED DESCRIPTION

[0046] The technical solutions in the embodiments of the present application will be described clearly and completely below with reference to the accompanying drawings in the embodiments of the present application. Obviously, the described embodiments are only part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative work fall within the scope of protection of the present application.

[0047] As shown in Figure 1, the present application provides a treatment method for sulfur-containing waste gas and waste liquid, which comprises the following steps: Figure 1

[0048] The pyrolysis incineration unit comprises a pyrolysis incineration furnace 1 and a waste heat recovery furnace 2.

[0049] ​Sulfur-containing waste gas, waste liquid is added to the inside of the cracking incinerator 1, and fuel gas and combustion air are injected into the inside of the cracking incinerator 1, which contains an igniter, not shown here, which ignites the fuel gas and combustion air through the igniter, achieving the effect of incineration, so that the sulfur-containing waste gas, waste liquid is cracked and incinerated to generate high-temperature steam containing sulfur dioxide. The sulfur-containing waste gas, waste liquid first undergoes thermal cracking at high temperature, releasing gaseous sulfide or elemental sulfur. The reducing sulfide generated by cracking is completely oxidized with oxygen at high temperature to generate sulfur dioxide. The high-temperature steam containing sulfur dioxide is cooled and heat energy is recovered in the waste heat recovery furnace 2. The heat inside can be recycled under the recovery of the waste heat recovery furnace 2, thereby achieving the effect of energy saving, so that the treatment is more environmentally friendly. The cracking incinerator 1 and the waste heat recovery furnace 2 are provided with temperature monitoring equipment for controlling the temperature of the process gas, so that the process gas treatment is controllable.

[0050] The catalytic oxidation unit includes a staged sulfur dioxide reactor 3, which uses a PTIL-WXP series catalyst:

[0051] The high-temperature steam containing sulfur dioxide enters the staged sulfur dioxide reactor 3, and the sulfur dioxide is oxidized to sulfur trioxide. Under the action of the PTIL-WXP catalyst, the sulfur dioxide and oxygen undergo catalytic oxidation to generate sulfur trioxide.

[0052] The condensation concentration unit includes a sulfuric acid condensate collection tank 4, a condenser 5, a sulfuric acid cooler 9, and a sulfuric acid storage tank 10:

[0053] The sulfur trioxide process gas is condensed into liquid sulfuric acid when it exchanges heat with air taken from the environment in the condenser 5 and flows into the sulfuric acid condensate collection tank 4 under the action of gravity. After cooling in the sulfuric acid cooler 9, it is stored in the sulfuric acid storage tank 10. The preliminary sulfuric acid liquid is prepared by condensation, thereby preliminary recovery of sulfur components. The gas is discharged from the top of the condenser 5 after condensation;

[0054] The tail gas purification unit includes a PTIL-CC reactor 6, a high-efficiency demister 7, and a chimney 8:

[0055] The process gas from the top of the condenser 5 enters the PTIL-CC reactor 6, and the residual sulfur dioxide gas in the PTIL-CC reactor 6 is oxidized to sulfur trioxide. The sulfur dioxide and oxygen undergo catalytic oxidation to generate sulfur trioxide under the action of the PTIL-CC catalyst, and the sulfur trioxide is washed with water in the PTIL-CC reactor 6 to form dilute acid. The gas converted to sulfur trioxide by the catalytic oxidation of the PTIL-CC catalyst is then washed inside the PTIL-CC reactor 6, and then forms dilute acid, which is further converted to sulfuric acid, further improving the conversion and recovery degree of sulfur, and finally becomes finished sulfuric acid flowing into the sulfuric acid storage tank 10. The process gas then enters the high-efficiency mist eliminator 7, which removes sulfur dioxide acid mist in the tail gas under the action of a high-voltage electric field. The flue gas is first cooled to below the acid dew point, such as 80-120℃, so that the SO3 is condensed into liquid sulfuric acid mist droplets, facilitating electrostatic capture. The high-efficiency mist eliminator 7 can be a wet electrostatic mist eliminator. The acid mist droplets are ionized by corona discharge, captured by the dust collector, and discharged from the chimney 8, thereby achieving ultra-clean emission that meets the tail gas emission index.

[0056] Please refer to Figure 1 The temperature of the pyrolysis incineration is controlled at 950-1050℃, and the pressure in the pyrolysis incinerator 1 is controlled at -1-0KPa micro-negative pressure. The high temperature of 950-1050℃ promotes pyrolysis and oxidation, ensuring that it is oxidized to sulfur dioxide.

[0057] Please refer to Figure 1 The outlet of the sectional sulfur dioxide reactor 3 is provided with a plate heat exchanger 14. The plate heat exchanger 14 uses high-pressure saturated steam / high-pressure saturated steam water to exchange heat with the process gas to take away the reaction heat. The use of high-pressure saturated steam / high-pressure saturated steam water enables the reaction heat to be taken away in time, improves the heat diffusion efficiency, and controls the temperature at the outlet of the catalytic oxidation unit. The inlet temperature of the sectional sulfur dioxide reactor 3 is controlled at 380-420℃, and the outlet temperature of the catalytic oxidation unit is controlled at 270-290℃. The waste heat recovery furnace 2 can take away the heat generated after incineration to control the inlet temperature of the sectional sulfur dioxide reactor 3, and the pressure is controlled at 0-1KPa micro-positive pressure.

[0058] Please refer to Figure 1 The process gas side of the condenser 5 is maintained at -1-0KPa micro-negative pressure to reduce the boiling point of water in the process and take away more water to control the concentration of sulfuric acid. The outlet temperature of the condenser 5 is controlled at 90-110℃.

[0059] Please refer to Figures 1 to 4, the device comprises a cracking incinerator 1, a waste heat recovery furnace 2, a sectional sulfur dioxide reactor 3, a sulfuric acid condensate collecting tank 4, a condenser 5, a PTIL-CC reactor 6, a high-efficiency demister 7, a chimney 8, a sulfuric acid cooler 9, a sulfuric acid storage tank 10, a device mounting support 11;

[0060] The cracking incinerator 1, the waste heat recovery furnace 2, the sectional sulfur dioxide reactor 3, the sulfuric acid condensate collecting tank 4, the condenser 5, the PTIL-CC reactor 6, the high-efficiency demister 7, the chimney 8, the sulfuric acid cooler 9, and the sulfuric acid storage tank 10 are all mounted above the device mounting support 11, and the top of the cracking incinerator 1 is provided with a feeding pipe and gas inlets for injecting fuel gas and combustion air, so that the fuel gas and the combustion air can crack and incinerate the process gas in the cracking incinerator 1.

[0061] A flow guide heat dissipation pipe 12 for discharging process gas is mounted on the top of the outer surface of the cracking incinerator 1, and the high-temperature sulfur dioxide vapor formed by cracking and incineration enters the waste heat recovery furnace 2 from the flow guide heat dissipation pipe 12 to recover waste heat and cool the high-temperature sulfur dioxide vapor, so as to control the temperature of the high-temperature sulfur dioxide vapor to a temperature suitable for the reaction of sulfur dioxide into sulfur trioxide, thereby ensuring the reaction effect.

[0062] Please refer to Figures 1 to 5 The waste heat recovery furnace 2 comprises a waste heat recovery furnace body 2a, an outer layer sandwich cavity 2b, an inner cavity 2c, and a flow guide cyclone vane 2d.

[0063] A cylindrical partition is mounted in the middle of the waste heat recovery furnace body 2a, which separates the inside of the cracking incinerator furnace body 1a into two parts, the outer layer sandwich cavity 2b and the inner cavity 2c, and the flow guide cyclone vane 2d is mounted at the lower part of the inner cavity 2c. The flow guide heat dissipation pipe 12 extends into the outer layer sandwich cavity 2b from top to bottom and is connected with the inner cavity 2c. When the flow guide heat dissipation pipe 12 passes through the outer layer sandwich cavity 2b, it can dissipate heat and form air cyclone under the action of the flow guide cyclone vane 2d, so that the process gas can fully contact with the inner wall of the inner cavity 2c, ensuring the cooling effect. The gas outlet of the flow guide heat dissipation pipe 12 is below the flow guide cyclone vane 2d.

[0064] The flow guide heat dissipation pipe 12 comprises a main pipe 12a and branch pipes 12b, the branch pipes 12b are combined to form a pipeline and are connected with the main pipe 12a, and the branch pipes 12b are in the outer layer sandwich cavity 2b.

[0065] Please refer to Figures 1 to 6 and Figure 8 The sectional sulfur dioxide reactor 3 comprises a first reaction tank body 3a, a catalyst bed 3b, a flow distribution layer plate 3c, a self-adaptive upper top frame 3d, springs 3e, and a mounting and dismounting pull-out frame 13.

[0066] The inside of the first reaction tank body 3a is vertically provided with a mounting slot matched with the catalyst bed layer 3b, the shunt layer plate 3c and the adaptive upper top frame 3d outer frame. The catalyst bed layer 3b, the shunt layer plate 3c and the adaptive upper top frame 3d outer frame are the same, so that the catalyst bed layer 3b and the shunt layer plate 3c can be stacked in the inside of the first reaction tank body 3a, thereby forming the effect of segmented reaction. The mounting and dismounting pull-out frame 13 is pullably mounted on the top of the mounting slot. By the mounting and dismounting pull-out frame 13, the catalyst bed layer 3b and the shunt layer plate 3c can be mounted from above. The mounting and dismounting pull-out frame 13 is hollow in the middle and is the same as the catalyst bed layer 3b, the shunt layer plate 3c and the adaptive upper top frame 3d outer frame, so that the catalyst bed layer 3b and the shunt layer plate 3c can be in the middle of the mounting and dismounting pull-out frame 13, and the pushing of the mounting and dismounting pull-out frame 13 can drive the catalyst bed layer 3b and the shunt layer plate 3c to be mounted,

[0067] The middle part of the shunt layer plate 3c is gradually downwardly arc-shaped from the middle to the outside, and the middle part of the shunt layer plate 3c is provided with a ventilation hole. The process gas passing through the shunt layer plate 3c can be relatively uniformly passed through the catalyst bed layer 3b, avoiding the concentrated treatment of the process gas, so that the treatment effect is better,

[0068] The catalyst bed layer 3b and the shunt layer plate 3c are placed in intervals. The adaptive upper top frame 3d is installed at the bottommost part and can abut against the outer frame of the bottommost catalyst bed layer 3b. Under the action of the spring 3e, the catalyst bed layer 3b and the shunt layer plate 3c can be adaptively relatively limited after being mounted. The bottom of the adaptive upper top frame 3d is connected with the spring 3e. The bottom end of the spring 3e is mounted at the bottom of the mounting slot. Under the action of the elasticity of the spring 3e, the adaptive upper top frame 3d can be provided with a jacking force.

[0069] Please refer to Figures 1 to 8 , the condenser 5 comprises a condenser main body 5a and a glass condenser tube 5b;

[0070] The glass condenser tube 5b is installed in the inside of the condenser main body 5a and is spiral-shaped, so that the contact area is wider, thereby making the condensation effect better. Through the spiral design, the upward process gas can fully contact the inner wall of the glass condenser tube 5b, thereby making the condensation effect better.

[0071] Please refer to Figures 1 to 8 , the PTIL-CC reactor 6 comprises a second reaction tank body 6a, a water spraying pipeline 6b, a PTIL-CC catalyst bed layer 6c and a cylindrical cylinder 6d;

[0072] A cylinder 6d is installed in the middle of the inner top of the second reactor 6a, and the cylinder 6d is in communication with the gas outlet. The bottom end of the cylinder 6d is in a suspended state. The PTIL-CC catalytic bed 6c is installed between the inner wall of the second reactor 6a and the outer wall of the cylinder 6d. The process gas first passes through the PTIL-CC catalytic bed 6c from top to bottom between the inner wall of the second reactor 6a and the outer wall of the cylinder 6d. Then, the reacted sulfur trioxide moves from the cylinder 6d to the water spraying pipeline 6b from bottom to top. Then, under the water washing of the water spraying pipeline 6b, the dilute acid is formed,

[0073] The top end of the inner wall of the cylinder 6d is provided with the water spraying pipeline 6b.

[0074] Although the embodiments of the present application have been shown and described, it is to be understood that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the present application, and the scope of the present application is defined by the appended claims and their equivalents.

Claims

1. A method for treating sulfur-containing waste gas and waste liquid, characterized in that, The method includes: The pyrolysis incineration unit includes a pyrolysis incinerator (1) and a waste heat recovery furnace (2): Sulfur-containing waste gas and waste liquid are added to the interior of the pyrolysis incinerator (1), and fuel gas and combustion air are injected into the interior of the pyrolysis incinerator (1) to pyrolyze and incinerate the sulfur-containing waste gas and waste liquid to generate high-temperature steam containing sulfur dioxide. The high-temperature steam containing sulfur dioxide is cooled and the heat energy is recovered by the waste heat recovery furnace (2). The catalytic oxidation unit includes a segmented sulfur dioxide reactor (3), which uses a PTIL-WXP series catalyst. High-temperature steam containing sulfur dioxide enters the segmented sulfur dioxide reactor (3), where the sulfur dioxide is oxidized into sulfur trioxide; The condensation and concentration unit includes a sulfuric acid condensate collection tank (4), a condenser (5), a sulfuric acid cooler (9), and a sulfuric acid storage tank (10). When the sulfur trioxide process gas exchanges heat with the air taken from the environment in the condenser (5), it is condensed into liquid sulfuric acid and flows into the sulfuric acid condensate collection tank (4) under the action of gravity. After being cooled by the sulfuric acid cooler (9), it is stored in the sulfuric acid storage tank (10). The exhaust gas purification unit includes a PTIL-CC reactor (6), a high-efficiency demister (7), and a chimney (8). The process gas coming out from the top of the condenser (5) enters the PTIL-CC reactor (6), where the residual sulfur dioxide gas is oxidized to sulfur trioxide. The sulfur trioxide is then washed with water in the PTIL-CC reactor (6) to become dilute acid, which eventually becomes finished sulfuric acid and flows into the sulfuric acid storage tank (10). The process gas then enters the high-efficiency demister (7), where sulfuric acid trioxide mist is removed from the tail gas under the action of a high-voltage electric field and discharged from the chimney (8). The PTIL-CC reactor (6) includes a second reaction tank (6a), a water spray line (6b), a PTIL-CC catalyst bed (6c), and a cylindrical tube (6d); A cylindrical tube (6d) is installed in the middle of the top of the second reaction vessel (6a), and the cylindrical tube (6d) is connected to the gas outlet. The bottom end of the cylindrical tube (6d) is suspended. The PTIL-CC catalyst bed (6c) is installed between the inner wall of the second reaction vessel (6a) and the outer wall of the cylindrical tube (6d). A water spray line (6b) is installed at the top of the inner wall of the cylindrical tube (6d).

2. The method for treating sulfur-containing waste gas and waste liquid according to claim 1, characterized in that: The temperature of the pyrolysis incineration is controlled at 950-1050℃, and the pressure inside the pyrolysis incinerator (1) is controlled at a slight negative pressure of -1 to 0KPa.

3. The method for treating sulfur-containing waste gas and waste liquid according to claim 2, characterized in that: The outlet of the segmented sulfur dioxide reactor (3) is equipped with a plate heat exchanger (14). The plate heat exchanger (14) uses high-pressure saturated steam / high-pressure saturated steam water and process gas to transfer the reaction heat. The inlet temperature of the segmented sulfur dioxide reactor (3) is controlled between 380 and 420°C, the outlet temperature of the catalytic oxidation unit is controlled between 270 and 290°C, and the pressure is controlled at a slight positive pressure of 0 to 1 kPa.

4. The method for treating sulfur-containing waste gas and waste liquid according to claim 3, characterized in that: The process gas side of the condenser (5) is maintained at a slight negative pressure of -1 to 0 kPa, and the outlet temperature of the condenser (5) is controlled at 90 to 110°C.

5. A treatment device for sulfur-containing waste gas and waste liquid using the method of any one of claims 1-4, characterized in that: The equipment includes a pyrolysis incinerator (1), a waste heat recovery furnace (2), a segmented sulfur dioxide reactor (3), a sulfuric acid condensate collection tank (4), a condenser (5), a PTIL-CC reactor (6), a high-efficiency demister (7), a chimney (8), a sulfuric acid cooler (9), a sulfuric acid storage tank (10), and an equipment mounting bracket (11). The pyrolysis incinerator (1), waste heat recovery furnace (2), segmented sulfur dioxide reactor (3), sulfuric acid condensate collection tank (4), condenser (5), PTIL-CC reactor (6), high-efficiency demister (7), chimney (8), sulfuric acid cooler (9), and sulfuric acid storage tank (10) are all installed above the equipment mounting bracket (11). The top of the pyrolysis incinerator (1) is provided with a feed pipe and an air inlet for injecting fuel gas and combustion air. The top of the outer surface of the pyrolysis incinerator (1) is equipped with a heat dissipation pipe (12) for supplying process gas. The pyrolysis incinerator (1), waste heat recovery furnace (2), segmented sulfur dioxide reactor (3), and condenser (5) are connected in sequence by pipes. The sulfuric acid condensate collection tank (4), sulfuric acid cooler (9), and sulfuric acid storage tank (10) are connected in sequence by pipes. The outlet of the condenser (5) is connected to the sulfuric acid condensate collection tank (4) by pipes. The outlet of the PTIL-CC reactor (6) is connected to the sulfuric acid storage tank (10) by pipes. The outlet of the condenser (5) is connected to the PTIL-CC reactor (6) by pipes. The outlet of the PTIL-CC reactor (6), the high-efficiency demister (7), and the chimney (8) are connected in sequence by pipes.

6. The treatment equipment for sulfur-containing waste gas and waste liquid according to claim 5, characterized in that: The waste heat recovery furnace (2) includes a furnace body (2a), an outer jacket (2b), an inner cavity (2c), and guide swirl blades (2d); A cylindrical partition is installed in the middle of the furnace body (2a) of the waste heat recovery furnace, which divides the interior of the furnace body (2a) into two parts: an outer cavity (2b) and an inner cavity (2c). A flow guide swirl vane (2d) is installed at the lower part of the inner cavity (2c). The flow guide heat dissipation pipe (12) extends from top to bottom into the outer cavity (2b) and is connected to the inner cavity (2c). The air outlet of the flow guide heat dissipation pipe (12) is located below the flow guide swirl vane (2d). The heat dissipation pipe (12) includes a main pipe (12a) and branch pipes (12b). The branch pipes (12b) are combined to form a pipeline and are connected to the main pipe (12a). The branch pipes (12b) are located in the outer cavity (2b).

7. The treatment equipment for sulfur-containing waste gas and waste liquid according to claim 6, characterized in that: The segmented sulfur dioxide reactor (3) includes a first reaction tank (3a), a catalyst bed (3b), a flow divider (3c), an adaptive top frame (3d), a spring (3e), and an installation and disassembly pull-out bracket (13); The first reaction vessel (3a) has vertically formed mounting slots inside, which are adapted to the catalyst bed (3b), the flow divider plate (3c), and the outer frame of the adaptive top frame (3d). The catalyst bed (3b), the flow divider plate (3c), and the outer frame of the adaptive top frame (3d) are identical. The installation and disassembly pull-out bracket (13) is removable and installed on the top of the mounting slot. The middle of the installation and disassembly pull-out bracket (13) is hollow, and it is identical to the outer frame of the catalyst bed (3b), the flow divider plate (3c), and the outer frame of the adaptive top frame (3d). The middle portion of the flow divider plate (3c) has an arc-shaped structure that gradually descends from the outer center, and ventilation holes are provided in the middle portion of the flow divider plate (3c). The catalyst bed (3b) and the flow divider plate (3c) are placed at intervals. The adaptive top frame (3d) is installed at the bottom and can abut against the outer frame of the bottom catalyst bed (3b). A spring (3e) is connected to the bottom of the adaptive top frame (3d), and the bottom end of the spring (3e) is installed at the bottom of the mounting groove.

8. The treatment equipment for sulfur-containing waste gas and waste liquid according to claim 7, characterized in that: The condenser (5) includes a condenser body (5a) and a glass condenser tube (5b); The glass condenser tube (5b) is installed inside the condenser body (5a) and is spiral in shape.

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