Method and equipment for treating sulfur-containing waste gas and waste liquid

Abstract

The invention discloses a sulfur-containing waste gas and waste liquid treatment method and equipment, and particularly relates to the technical field of sulfur-containing waste gas and waste liquid treatment.The sulfur-containing waste gas and waste liquid treatment method is characterized in that a cracking incineration unit, a catalytic oxidation unit, a condensation and concentration unit and a tail gas purification unit are included; sulfur-containing waste gas and waste liquid are sequentially cracked and incinerated into sulfur dioxide, then converted into sulfur trioxide and condensed to form sulfuric acid, sulfur dioxide in tail gas is converted and washed to form dilute acid, sulfuric acid trioxide mist in the tail gas is removed under the action of a high-voltage electric field, and the tail gas is discharged from a chimney. And the effects of ultra-clean emission and high total sulfur recovery rate are achieved under the condition of meeting tail gas emission indexes.

Description

Technical Field

[0001] The present invention relates to the technical field of treatment of sulfur-containing waste gas and waste liquid, and in particular to a method and equipment for treating sulfur-containing waste gas and waste liquid. Background Art

[0002] Currently, sulfur-containing waste gas treatment primarily involves physical, chemical, and biological methods. Physical methods include adsorption and condensation. While both require simple equipment, they suffer from low treatment efficiency, high operating costs, and the potential for secondary pollution. Chemical methods primarily include absorption and catalytic combustion. Absorption suffers from high investment and operating costs, and the potential for generating large amounts of secondary waste. Catalytic combustion also has high operating costs and requires rigorous waste gas pretreatment. Biological methods are subject to significant limitations, including geographical location, seasonality, and operating conditions, resulting in low purification efficiency.

[0003] The current disposal technologies for sulfur-containing waste liquid include acid recovery method, precipitation method, biochemical treatment method and oxidation method. The acid recovery method has high requirements on the sealing and corrosion resistance of the equipment, high investment and poor promotion; the precipitation method has poor precipitation of the product and high treatment cost; the biochemical treatment method has high requirements on the water quality of the waste liquid, long treatment time, and the microorganisms are easily impacted; the oxidation method is divided into direct oxidation and catalytic oxidation. Direct oxidation is suitable for occasions with low sulfur content. The disadvantage is that the treatment cost is high and the oxidant poses a safety risk; catalytic oxidation is suitable for high-concentration sulfur-containing wastewater, has high reaction conditions, and requires continuous addition of catalysts. To this end, we propose a treatment method and equipment for sulfur-containing waste gas and waste liquid to solve the above problems. Summary of the Invention

[0004] The purpose of the present invention is to provide a method and equipment for treating sulfur-containing waste gas and waste liquid to solve the problems raised in the above background technology.

[0005] To achieve the above object, the present invention provides the following technical solution: a method for treating sulfur-containing waste gas and waste liquid, characterized in that the method comprises:

[0006] The pyrolysis incineration unit includes a pyrolysis incinerator and a waste heat recovery furnace:

[0007] Add sulfur-containing waste gas and waste liquid to the interior of the pyrolysis incinerator, and inject fuel gas and combustion-supporting air into the interior of the pyrolysis incinerator to cause the sulfur-containing waste gas and waste liquid to be pyrolyzed and incinerated to generate high-temperature steam containing sulfur dioxide. The high-temperature steam containing sulfur dioxide is cooled and heat energy is recovered by the waste heat recovery furnace;

[0008] The catalytic oxidation unit includes a segmented sulfur dioxide reactor, which uses a PTIL-WXP series catalyst:

[0009] High-temperature steam containing sulfur dioxide enters the staged sulfur dioxide reactor, where the sulfur dioxide is oxidized into sulfur trioxide;

[0010] Condensation and concentration unit, which includes 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 when exchanging heat with the air taken from the environment in the condenser and flows into the sulfuric acid condensate collection tank under the action of gravity. It is then cooled in the sulfuric acid cooler and stored in the sulfuric acid storage tank.

[0012] Tail gas purification unit, which includes a PTIL-CC reactor, a high-efficiency demister, and a chimney:

[0013] The process gas coming out of the top of the condenser enters the PTIL-CC reactor, where the remaining sulfur dioxide gas is oxidized into sulfur trioxide and washed with water to become dilute acid. It eventually becomes finished sulfuric acid and flows into the sulfuric acid storage tank. The process gas then enters the high-efficiency demister, where the sulfuric acid dioxide mist in the tail gas is removed under the action of a high-voltage electric field and discharged from the chimney.

[0014] Preferably, the temperature of the pyrolysis incineration is controlled at 950 to 1050° C., and the pressure in the pyrolysis incineration furnace is controlled at a slightly negative pressure of -1 to 0 KPa.

[0015] Preferably, a plate heat exchanger is provided at the outlet of the segmented sulfur dioxide reactor, and the plate heat exchanger uses high-pressure saturated steam / high-pressure saturated steam water to exchange heat with the process gas to remove the reaction heat. The inlet temperature of the segmented sulfur dioxide reactor 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 slightly positive pressure of 0 to 1 KPa.

[0016] Preferably, the process gas side of the condenser is maintained at a slight negative pressure of -1 to 0 KPa, and the condenser outlet temperature is controlled at 90 to 110°C.

[0017] Preferably, the equipment includes a cracking incinerator, a waste heat recovery furnace, a segmented sulfur dioxide reactor, a sulfuric acid condensate collection tank, a condenser, a PTIL-CC reactor, a high-efficiency demister, a chimney, a sulfuric acid cooler, a sulfuric acid storage tank, and an equipment mounting bracket;

[0018] The pyrolysis incinerator, waste heat recovery furnace, segmented sulfur dioxide reactor, sulfuric acid condensate collection tank, condenser, PTIL-CC reactor, high-efficiency demister, chimney, sulfuric acid cooler, and sulfuric acid storage tank are all installed above the equipment mounting bracket. The top of the pyrolysis incinerator is provided with a feed pipe and an air port for injecting fuel gas and combustion-supporting air.

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

[0020] The top of the outer surface of the cracking incinerator is provided with a 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 guide swirl blades;

[0022] A cylindrical partition is installed in the middle of the waste heat recovery furnace body, which divides the interior of the pyrolysis incinerator body into an outer layer cavity and an inner cavity. A guide swirl blade is installed at the lower part of the inner cavity. The guide heat dissipation pipe extends from top to bottom into the outer layer cavity and is connected to the inner cavity. The air outlet of the guide heat dissipation pipe is located below the guide swirl blade.

[0023] The diversion heat dissipation pipe includes a main pipe and a branch pipe. The branch pipes are combined to form a pipeline and are connected to the main pipe. The branch pipes are located in the outer layer cavity.

[0024] Preferably, the segmented sulfur dioxide reactor includes a first reaction tank body, a catalyst bed, a diversion layer plate, an adaptive upper frame, a spring, and an installation and disassembly pull-out frame;

[0025] The interior of the first reaction tank body is vertically provided with an installation groove adapted to the catalyst bed, the diverter plate, and the outer frame of the adaptive top frame. The catalyst bed, the diverter plate, and the outer frame of the adaptive top frame are the same. The installation and disassembly pull-out frame can be installed in a pull-out manner on the top of the installation groove. The middle of the installation and disassembly pull-out frame is hollowed out and is the same as the catalyst bed, the diverter plate, and the outer frame of the adaptive top frame.

[0026] The middle part of the diversion layer plate is an arc-shaped structure that gradually extends downward from the middle outer side, and a ventilation hole is opened in the middle part of the diversion layer plate.

[0027] The catalyst bed and the diversion layer are placed at intervals. The adaptive upper frame is installed at the bottom and can abut against the outer frame of the bottom catalyst bed. The bottom of the adaptive upper frame is connected to a spring, and the bottom end of the spring is installed at the bottom of the installation groove.

[0028] Preferably, the condenser includes a condenser body and a glass condenser tube;

[0029] The glass condenser tube is installed inside the condenser body, and the glass condenser tube is spiral-shaped.

[0030] Preferably, the PTIL-CC reactor comprises a second reaction tank, a water spray line, a catalytic bed, and a cylindrical barrel;

[0031] A cylindrical tube is installed in the middle of the top of the second reaction tank body, and the cylindrical tube is connected to the gas outlet. The bottom end of the cylindrical tube is suspended in the air. The catalytic bed is installed between the inner wall of the second reaction tank body and the outer wall of the cylindrical tube.

[0032] A water spray pipeline is installed on the top end of the inner wall of the cylindrical barrel.

[0033] Compared with the prior art, the present invention has the following beneficial effects:

[0034] 1. Sulfur-containing waste gas and waste liquid are sequentially processed through the cracking and incineration unit, catalytic oxidation unit, condensation and concentration unit, and tail gas purification unit to convert them into sulfur dioxide gas. The sulfur dioxide gas is catalytically oxidized to become sulfur trioxide gas, which is hydrated to form sulfuric acid vapor and condensed to produce finished sulfuric acid. At the same time, the sulfur dioxide in the condensed tail gas can be used to produce sulfuric acid under the action of a low-temperature active catalyst, and the acid mist is removed in a high-efficiency demister, achieving ultra-clean emissions while meeting tail gas emission indicators and achieving a high total sulfur recovery rate.

[0035] 2. Through the cooperation of the adaptive upper frame and the spring, the number of catalyst beds can be changed according to the specific needs of use under the action of the installation and removal of the pull-out frame, which is convenient for use. The catalyst bed can be quickly replaced by pulling out the installation and removal of the pull-out frame, thereby facilitating its use. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0037] Figure 1 It is a schematic diagram of the process of the present invention.

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

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

[0040] Figure 4 It is a schematic diagram of the cross-sectional structure of the present invention.

[0041] Figure 5 It is a structural schematic diagram of the heat-conducting pipe in the present invention.

[0042] Figure 6 It is a structural schematic diagram of installing and disassembling the pull-out rack in the present invention.

[0043] Figure 7 It is a structural schematic diagram of the glass condenser in the present invention.

[0044] Figure 8 It is a structural diagram of the adaptive top frame in the present invention.

[0045] In the figure: 1. Cracking incinerator; 2. Waste heat recovery furnace; 2a. Waste heat recovery furnace body; 2b. Outer layer cavity; 2c. Inner cavity; 2d. Guide swirl blade; 3. Segmented sulfur dioxide reactor; 3a. First reaction tank; 3b. Catalyst bed; 3c. Diverter plate; 3d. Adaptive upper frame; 3e. Spring; 4. Sulfuric acid condensate collection tank; 5. Condenser; 5a. Condenser body; 5b. Glass condenser tube; 6. PTIL-CC reactor; 6a. Second reaction tank; 6b. Water spray pipeline; 6c. PTIL-CC catalytic bed; 6d. Cylinder; 7. High-efficiency demister; 8. Chimney; 9. Sulfuric acid cooler; 10. Sulfuric acid storage tank; 11. Equipment mounting bracket; 12. Guide heat dissipation pipe; 12a. Main pipe; 12b. Branch pipe; 13. Installation and disassembly pull-out rack; 14. Plate heat exchanger. DETAILED DESCRIPTION

[0046] The following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0047] like Figure 1 As shown, the present invention provides a method for treating sulfur-containing waste gas and waste liquid, the method comprising:

[0048] The pyrolysis incineration unit includes a pyrolysis incinerator 1 and a waste heat recovery furnace 2:

[0049] Sulfur-containing waste gas and waste liquid are added to the interior of the cracking incinerator 1, and fuel gas and combustion-supporting air are injected into the interior of the cracking incinerator 1. The cracking incinerator 1 contains an igniter, which is not shown here. The fuel gas and combustion-supporting air are ignited by the igniter to achieve the incineration effect, so that the sulfur-containing waste gas and waste liquid are cracked and incinerated to generate high-temperature steam containing sulfur dioxide. The sulfur-containing waste gas and waste liquid first undergo thermal cracking at high temperature to release 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 by the waste heat recovery furnace 2. The heat inside it can be recycled under the recovery of the waste heat recovery furnace 2, thereby achieving energy-saving effect, making its treatment 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 to achieve controllable process gas treatment;

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

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

[0052] Condensation and concentration unit, which 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 exchanging heat with the 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 performing preliminary recovery of the sulfur component. After condensation, the process gas is discharged from the top of the condenser 5.

[0054] Tail gas purification unit, which 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, where the residual sulfur dioxide gas is oxidized to sulfur trioxide. Under the action of the PTIL-CC catalyst, sulfur dioxide and oxygen undergo a catalytic oxidation reaction to form sulfur trioxide, which is then washed with water in the PTIL-CC reactor 6 to form dilute acid. The process gas is then catalytically oxidized to sulfur trioxide gas by the PTIL-CC catalyst, and then washed with water inside the PTIL-CC reactor 6 to form dilute acid, which is further converted into sulfuric acid. , further improving the conversion and recovery degree of sulfur, and finally becoming finished sulfuric acid flowing into the sulfuric acid storage tank 10, and then the process gas enters the high-efficiency demister 7, and the sulfuric acid dioxide mist in the tail gas is removed under the action of the high-voltage electric field. The flue gas is first cooled to below the acid dew point, such as 80-120°C, so that SO3 is condensed into liquid sulfuric acid droplets, which is convenient for electrostatic capture. The high-efficiency demister 7 can be a wet electrostatic demister, which ionizes the gas through corona discharge. The acid mist droplets are charged and captured by the dust collecting electrode and discharged from the chimney 8, thereby achieving ultra-clean emissions that meet the tail gas emission indicators.

[0056] See also Figure 1 The temperature of the cracking and incineration is controlled at 950-1050°C, and the pressure in the cracking and incineration furnace 1 is controlled at a slight negative pressure of -1-0KPa. The high temperature of 950-1050°C promotes cracking and oxidation, ensuring that it is oxidized to sulfur dioxide.

[0057] See also Figure 1 The outlet of the segmented 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 remove the reaction heat. The use of high-pressure saturated steam / high-pressure saturated steam water enables it to promptly remove the reaction heat, thereby improving its heat diffusion efficiency, so as to control the temperature at the outlet of the catalytic oxidation unit. The inlet temperature of the segmented sulfur dioxide reactor 3 is controlled between 380 and 420°C, and the outlet temperature of the catalytic oxidation unit is controlled between 270 and 290°C. The heat generated after incineration can be removed by the waste heat recovery furnace 2 to achieve the effect of controlling the inlet temperature of the segmented sulfur dioxide reactor 3, and the pressure is controlled at a slightly positive pressure of 0 to 1 kPa.

[0058] See also Figure 1 The process gas side of the condenser 5 is maintained at a slight negative pressure of -1 to 0 KPa to reduce the boiling point of water in the process and take away more water to achieve the control of sulfuric acid concentration. The outlet temperature of the condenser 5 is controlled at 90 to 110 ° C.

[0059] See also Figures 1 to 4The equipment includes a cracking 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;

[0060] The pyrolysis incinerator 1, the waste heat recovery furnace 2, the segmented sulfur dioxide reactor 3, the sulfuric acid condensate collection 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 installed above the equipment mounting bracket 11. The top of the pyrolysis incinerator 1 is provided with a feed pipe and an air port for injecting fuel gas and combustion-supporting air, so that the fuel gas and combustion-supporting air can crack and incinerate the process gas in the pyrolysis incinerator 1;

[0061] A guide heat dissipation pipe 12 for discharging process gas is installed on the top of the outer surface of the cracking incinerator 1. The high-temperature sulfur dioxide steam formed by cracking and incineration enters the waste heat recovery furnace 2 from the guide heat dissipation pipe 12 for waste heat recovery, and the high-temperature sulfur dioxide steam is cooled to control the temperature of the high-temperature sulfur dioxide steam to reach a temperature suitable for the reaction of sulfur dioxide to sulfur trioxide, thereby ensuring the effect of the reaction.

[0062] See also Figures 1 to 5 The waste heat recovery furnace 2 includes a waste heat recovery furnace body 2a, an outer layer cavity 2b, an inner cavity 2c, and a guide swirl blade 2d;

[0063] A cylindrical partition is installed in the middle of the interior of the waste heat recovery furnace body 2a, and the interior of the cracking incinerator body 1a is divided into two parts, an outer layer cavity 2b and an inner cavity 2c, by the partition. A guide swirl blade 2d is installed at the lower part of the inner cavity 2c. The guide heat dissipation pipe 12 extends from top to bottom into the outer layer cavity 2b and is connected to the inner cavity 2c. The guide heat dissipation pipe 12 can dissipate heat when passing through the outer layer cavity 2b, and under the action of the guide swirl blade 2d, an air swirl can be formed, thereby allowing the process gas to fully contact the inner wall of the inner cavity 2c, ensuring its cooling effect. The air outlet of the guide heat dissipation pipe 12 is below the guide swirl blade 2d;

[0064] The heat dissipation pipe 12 includes a main pipe 12a and a branch pipe 12b. The branch pipe 12b is combined to form a pipe and is connected to the main pipe 12a. The branch pipe 12b is located in the outer layer cavity 2b.

[0065] See also Figures 1 to 6 and Figure 8 The segmented sulfur dioxide reactor 3 includes a first reaction tank 3a, a catalyst bed 3b, a diversion layer 3c, an adaptive upper frame 3d, a spring 3e and an installation and disassembly pull-out frame 13;

[0066] The interior of the first reaction tank body 3a is vertically provided with an installation groove adapted to the catalyst bed 3b, the diverter layer 3c, and the outer frame of the adaptive top frame 3d. The catalyst bed 3b, the diverter layer 3c, and the outer frame of the adaptive top frame 3d are the same, so that the catalyst bed 3b and the diverter layer 3c can be stacked inside the first reaction tank body 3a, thereby forming a staged reaction effect. The installation and disassembly pull-out rack 13 can be installed in a pull-out manner on the top of the installation groove. By installing and disassembling the pull-out rack 13, the catalyst bed 3b and the diverter layer 3c can be installed on the top. The middle of the installation and disassembly pull-out rack 13 is hollow, and it is the same as the catalyst bed 3b, the diverter layer 3c, and the outer frame of the adaptive top frame 3d, so that the catalyst bed 3b and the diverter layer 3c can be in the middle, so that the pushing of the installation and disassembly pull-out rack 13 can drive the catalyst bed 3b and the diverter layer 3c to be installed.

[0067] The middle part of the diverter plate 3c is in an arc-shaped structure that gradually extends downward from the middle outer side, and a vent hole is provided in the middle part of the diverter plate 3c. Under the guidance of the diverter plate 3c structure, the process gas can pass through the catalyst bed 3b relatively evenly, avoiding centralized treatment of the process gas, thereby achieving a better treatment effect.

[0068] The catalyst bed 3b and the diverter plate 3c are placed at intervals, and the adaptive upper frame 3d is installed at the bottom and can be abutted against the outer frame of the bottom catalyst bed 3b. Through the action of the spring 3e, the catalyst bed 3b and the diverter plate 3c can be adaptively restricted relative to each other after installation. The bottom of the adaptive upper frame 3d is connected to the spring 3e, and the bottom end of the spring 3e is installed at the bottom of the installation groove. Under the action of the elastic force of the spring 3e, it can provide the adaptive upper frame 3d with an upper force.

[0069] See also Figures 1 to 8 , the condenser 5 includes a condenser body 5a and a glass condenser tube 5b;

[0070] The glass condenser tube 5b is installed inside the condenser body 5a, and the glass condenser tube 5b is spiral-shaped, so that its contact area is wider, thereby making its 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 its condensation effect better.

[0071] See also Figures 1 to 8 The PTIL-CC reactor 6 includes a second reaction tank 6a, a water spray pipeline 6b, a PTIL-CC catalytic bed 6c, and a cylindrical barrel 6d;

[0072] A cylindrical barrel 6d is installed in the middle of the top of the second reaction tank body 6a, and the cylindrical barrel 6d is connected to the gas outlet. The bottom end of the cylindrical barrel 6d is suspended. The PTIL-CC catalytic bed 6c is installed between the inner wall of the second reaction tank body 6a and the outer wall of the cylindrical barrel 6d. The process gas first passes through the PTIL-CC catalytic bed 6c from top to bottom between the inner wall of the second reaction tank body 6a and the outer wall of the cylindrical barrel 6d, and then the reacted sulfur trioxide moves from bottom to top from the inside of the cylindrical barrel 6d to the water spray line 6b, and then forms dilute acid under the water washing of the water spray line 6b.

[0073] A water spraying pipeline 6b is installed at the top of the inner wall of the cylindrical tube 6d.

[0074] While embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions, and variations may be made to these embodiments without departing from the principles and spirit of the invention, and that the scope of the invention 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 comprises: A cracking and incineration unit, comprising a cracking and incineration furnace (1) and a waste heat recovery furnace (2): Sulfur-containing waste gas and waste liquid are added to the interior of a cracking incinerator (1), and fuel gas and combustion-supporting air are injected into the interior of the cracking incinerator (1) to crack 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 heat energy is recovered by passing through a waste heat recovery furnace (2); The catalytic oxidation unit comprises a segmented sulfur dioxide reactor (3), wherein the segmented sulfur dioxide reactor (3) adopts 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; A condensation and concentration unit, comprising a sulfuric acid condensate collecting tank (4), a condenser (5), a sulfuric acid cooler (9), and a sulfuric acid storage tank (10): The sulfur trioxide process gas is condensed into liquid sulfuric acid in the condenser (5) when exchanging heat with air taken from the environment and flows into the sulfuric acid condensate collection tank (4) under the action of gravity. After cooling in the sulfuric acid cooler (9), the sulfuric acid is stored in the sulfuric acid storage tank (10); The tail gas purification unit includes a PTIL-CC reactor (6), a high-efficiency demister (7), and a chimney (8): The process gas from the top of the condenser (5) enters the PTIL-CC reactor (6), where the remaining sulfur dioxide gas is oxidized to sulfur trioxide. The gas is then washed with water in the PTIL-CC reactor (6) to become dilute acid, and finally 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 the gas is discharged from the chimney (8).

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

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 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 remove 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 micro-positive pressure of 0 to 1KPa.

4. The method for treating sulfur-containing waste gas and waste liquid according to claim 4, 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, characterized by: The equipment comprises a cracking incinerator (1), a waste heat recovery furnace (2), a segmented 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), and an equipment mounting bracket (11); The cracking incinerator (1), the waste heat recovery furnace (2), the segmented 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 installed above the equipment mounting bracket (11), and the top of the cracking incinerator (1) is provided with a feed pipe and an air port for injecting fuel gas and combustion-supporting air; A guide and heat dissipation pipe (12) for discharging process gas is installed on the top of the outer surface of the cracking incinerator (1).

6. The sulfur-containing waste gas and waste liquid treatment equipment according to claim 6, characterized in that: The waste heat recovery furnace (2) comprises a waste heat recovery furnace body (2a), an outer layer cavity (2b), an inner cavity (2c), and guide swirl blades (2d); A cylindrical partition is installed in the middle of the waste heat recovery furnace body (2a), and the interior of the cracking incinerator body (1a) is divided into two parts, an outer layer cavity (2b) and an inner cavity (2c) by the partition. A guide swirl blade (2d) is installed at the lower part of the inner cavity (2c). The guide heat dissipation pipe (12) extends from top to bottom into the outer layer cavity (2b) and is connected to the inner cavity (2c). The air outlet of the guide heat dissipation pipe (12) is located below the guide swirl blade (2d); The heat conduction pipe (12) comprises a main pipe (12a) and a branch pipe (12b); the branch pipe (12b) is combined to form a pipe and is connected to the main pipe (12a); the branch pipe (12b) is located in the outer layer cavity (2b).

7. The sulfur-containing waste gas and waste liquid treatment equipment according to claim 7, characterized in that: The segmented sulfur dioxide reactor (3) comprises a first reaction tank body (3a), a catalyst bed (3b), a diversion layer plate (3c), an adaptive upper frame (3d), a spring (3e), and an installation and disassembly pull-out frame (13); The interior of the first reaction tank body (3a) is vertically provided with a mounting groove adapted to the outer frame of the catalyst bed (3b), the diverter plate (3c), and the adaptive upper frame (3d); the outer frames of the catalyst bed (3b), the diverter plate (3c), and the adaptive upper frame (3d) are identical; the mounting and dismounting pull-out rack (13) can be mounted on the top of the mounting groove in a pull-out manner; the middle of the mounting and dismounting pull-out rack (13) is hollowed out, and is identical to the outer frames of the catalyst bed (3b), the diverter plate (3c), and the adaptive upper frame (3d); The middle portion of the diversion layer plate (3c) is in an arc-shaped structure that gradually extends downward from the middle outer side, and a ventilation hole is provided in the middle portion of the diversion layer plate (3c). The catalyst bed (3b) and the diversion layer plate (3c) are placed at intervals, the self-adaptive top frame (3d) is installed at the bottom and can abut against the outer frame of the bottom catalyst bed (3b), the bottom of the self-adaptive top frame (3d) is connected to a spring (3e), and the bottom end of the spring (3e) is installed at the bottom of the installation groove.

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

9. The sulfur-containing waste gas and waste liquid treatment equipment according to claim 9, characterized in that: The PTIL-CC reactor (6) comprises a second reaction tank (6a), a water spray pipeline (6b), a PTIL-CC catalytic bed (6c), and a cylindrical barrel (6d); A cylindrical tube (6d) is installed in the middle of the top of the second reaction tank body (6a), and the cylindrical tube (6d) is communicated with the gas outlet in opposite directions. The bottom end of the cylindrical tube (6d) is suspended in the air. The PTIL-CC catalytic bed (6c) is installed between the inner wall of the second reaction tank body (6a) and the outer wall of the cylindrical tube (6d). A water spraying pipeline (6b) is installed at the top end of the inner wall of the cylindrical barrel (6d).

Images