System and device for recycling Claus tail gas

Abstract

The invention discloses a Claus tail gas recycling system and device, and relates to the technical field of Claus tail gas recycling. The method comprises the following steps that S1, firstly, the Claus tail gas is subjected to tail gas incineration to become SO2; s2, the process gas is cooled and then enters a sectional type SO reactor in a catalytic oxidation unit to be subjected to a catalytic oxidation reaction, and SO2 gas is oxidized into SO3; s3, the process gas enters a condensation acid-forming unit, and sulfuric acid steam is condensed into liquid sulfuric acid during heat exchange; by arranging the tail gas incineration unit, the catalytic oxidation unit, the condensation acid forming unit, the tail gas purification unit and the cracking unit, tail gas of the Claus device is incinerated, sulfur-containing substances are oxidized into SO2, SO2 is catalytically oxidized into SO3, hydration and condensation are performed to produce a finished product sulfuric acid, residual SO2 in the tail gas is converted into sulfuric acid under the action of a low-temperature active catalyst, and the tail gas is recycled. Acid mist is removed by a high-efficiency demister, the finished product sulfuric acid enters a vertical cracking furnace to be cracked into SO2, and the SO2 enters a Claus unit to be matched with hydrogen sulfide in proportion to produce sulfur.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of Claus tail gas regeneration and utilization, in particular to a system and device for Claus tail gas regeneration and utilization. BACKGROUND

[0002] Currently, there are various methods for treating Claus tail gas, each having advantages and disadvantages. The reduction absorption process uses hydrogen reduction to reduce sulfur components and then absorbs them by amine method, which has a complex process, high equipment and operation cost. The oxidation absorption process oxidizes sulfides into SO2 and then absorbs them by solvent, which has high device investment, is prone to side reactions, is difficult to operate and has high cost, and is less applied. The low-temperature Claus process generates sulfur at the sulfur dew point, which has high requirements for reaction conditions and equipment, high investment and operation cost, and is prone to pipeline blockage. The liquid-phase direct oxidation process converts H2S into elemental S using chelated iron solution at normal temperature and low pressure, but has limited treatment capacity, is not suitable for large-scale treatment, and has high operation cost due to frequent replacement of reagents. The Shell Claus tail gas treatment process has high sulfur recovery rate, low emission and strong flexibility, but may have high catalyst cost. Therefore, there is an urgent need to design a simple and efficient Claus tail gas regeneration system suitable for large-scale treatment. In addition, in the oxidation reaction of the tail gas, the oxidation layer may have reduced activity with use, and the oxidation layer needs to be replaced. In the traditional process, the catalyst needs to be replaced, which will cause production interruption, affect yield and economic benefit. To solve the above problems, the present application provides a system and device for Claus tail gas regeneration and utilization. SUMMARY

[0003] To solve the problems of large-scale and efficient treatment of Claus tail gas and replacement of catalysts without shutdown, the present application aims to provide a system and device for Claus tail gas regeneration and utilization.

[0004] To solve the above technical problems, the present application adopts the following technical solution: a system for Claus tail gas regeneration and utilization, comprising the following steps:

[0005] S1. First, the Claus tail gas enters a multi-fuel incinerator in a tail gas incineration unit, and becomes SO2 after incineration. The high-temperature process gas exits the incinerator and enters a waste heat recovery furnace to produce high-pressure saturated steam.

[0006] S2. After the process gas is cooled, it enters a staged SO reactor in a catalytic oxidation unit for catalytic oxidation reaction. The PTIL-WXP series catalyst in the reactor oxidizes SO2 gas into SO3. One or more bed layers are installed in the catalytic oxidation unit according to the change in the content of the raw material components.

[0007] S3, the process gas enters the condensing acid unit, the sulfuric acid vapor in the process gas is condensed into liquid sulfuric acid when heat exchanged with the air taken from the environment in the glass tube heat exchanger and flows into the sulfuric acid condensate collection tank under the action of gravity after being cooled by the heat exchanger and enters the cracking unit;

[0008] S4, the trace SO2 gas in the process gas from the glass tube condenser enters the tail gas purification unit for removal, and then the process gas enters the high-efficiency mist eliminator to remove SO3 acid mist in the tail gas, and the tail gas realizes ultra-clean emission under the most stringent emission index;

[0009] S5, the sulfuric acid produced by the condensing acid unit enters the vertical cracking furnace unique to the cracking unit, which cracks the sulfuric acid into SO2 gas, which is then pressurized by a compressor and sent to the Claus device condenser to produce sulfur or not cooled and sent to the Claus furnace as raw material to produce sulfur.

[0010] Preferably, the incinerator temperature in the tail gas incineration unit is controlled at 800-900℃, and the incinerator pressure is controlled at micro-negative pressure, at -1-0KPa.

[0011] Preferably, the outlet of each catalyst bed in the catalytic oxidation unit is equipped with a high-efficiency fin heat exchanger resistant to high-sulfur medium, and the fin 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 reactor catalyst bed inlet temperature is controlled between 380-435℃, the reactor outlet temperature is controlled between 270-290℃, and the pressure is controlled at micro-positive pressure.

[0012] Preferably, the glass tube heat exchanger in the condensing acid unit is confirmed to be set as one or more heat exchange modules according to the raw material, and the glass tube is in the form of a horizontal tube or a vertical tube, and a micro-negative pressure is maintained on the process gas side of the glass tube condenser to reduce the boiling point of water in the process, take away more water to control the concentration of sulfuric acid, and the outlet temperature of the glass tube condenser is controlled at 90-110℃.

[0013] Preferably, in the PTIL-CC reactor in the tail gas purification unit, the gas is oxidized to SO3 under the action of low-temperature active catalyst, washed with water to become dilute acid, and enters the condenser for concentration, and the temperature in the reactor is controlled below 80℃.

[0014] Preferably, the cracking temperature in the cracking unit is controlled at 900-1000℃, which cracks the sulfuric acid into SO2 gas, which is cooled to about 300℃ by a waste heat recovery furnace.

[0015] The device used by a system for recycling Claus tail gas comprises a support, three oxidation reaction bins and four through-bin pipes, the three oxidation reaction bins are vertically distributed and fixedly installed on the support, adjacent oxidation reaction bins are connected through the through-bin pipes to realize the transmission of gas between the oxidation reaction bins, adjacent two through-bin pipes are connected through a communication pipe, the through-bin pipe and the communication pipe are provided with three gas flow guide assemblies for changing the direction of gas, and the oxidation reaction bin is provided with an unfolding replacement assembly for replacing catalyst;

[0016] The gas flow guide assembly comprises two symmetrically distributed No. 1 isolation frames and No. 2 isolation frames, and the No. 1 isolation frame and the No. 2 isolation frame are respectively provided with a No. 1 air bag and a No. 2 air bag;

[0017] The unfolding replacement assembly comprises two symmetrically distributed fixed plates, the two fixed plates are fixedly installed on the inner wall of the oxidation reaction bin, a sliding frame is slidably arranged between the two fixed plates, and a catalyst layer is arranged in the sliding frame, two symmetrically distributed sliding plates are slidably arranged in the oxidation reaction bin, a guide rod is fixedly arranged between the two sliding plates, two symmetrically distributed connecting rods are rotatably arranged on the outer wall of the guide rod, and the top ends of the two connecting rods are connected with the sliding frame and the bottom ends are rotatably connected.

[0018] Preferably, the two No. 1 isolation frames are respectively located at the two ends of the oxidation reaction bin and are fixedly installed on the inner wall of the through-bin pipe between the oxidation reaction bin and the communication pipe, the No. 2 isolation frame is fixedly installed on the inner wall of the communication pipe, the inner walls of the No. 1 isolation frame and the No. 2 isolation frame are respectively fixedly provided with two symmetrically distributed No. 1 baffles and No. 2 baffles, a side plate is fixedly arranged on the outer wall of the support close to one side of the oxidation reaction bin, two symmetrically distributed pneumatic electromagnetic valves are fixedly arranged at the top end of the side plate, the No. 1 air bag and the No. 2 air bag are both provided with a gas guide pipe, and the other ends of the gas guide pipes of the No. 1 air bag and the No. 2 air bag are connected with the gas outlet ends of the pneumatic electromagnetic valves, and a gas source is arranged on one side of the support and connected with the pneumatic electromagnetic valves through the gas guide pipes.

[0019] Preferably, two symmetrically distributed transverse plates are fixedly arranged on the inner wall of the oxidation reaction bin, a guide column corresponding to the guide rod is fixedly arranged on the side of the sliding plate close to the transverse plate, a guide groove is arranged on the transverse plate, an arc-shaped groove is arranged on the side of the transverse plate away from the connecting rod, the arc-shaped groove is connected with the guide groove, the guide rod and the guide column slide in the arc-shaped groove and the guide groove, a drive shaft is rotatably arranged in the middle of the side of the oxidation reaction bin close to the guide column, a universal coupling is fixedly arranged at the inner end of the drive shaft, a screw rod is fixedly arranged at the other end of the universal coupling, a guide block is threadedly connected with the outer wall of the screw rod and rotatably arranged in the middle of the guide rod, door plates are fixedly arranged at the ends of the two sliding plates and used in cooperation with the oxidation reaction bin, a sealing strip is arranged at the closed connection between the door plates and the oxidation reaction bin, a blocking frame is arranged above the catalyst layer and fixedly connected with the sliding frame through bolts.

[0020] Compared with the prior art, the device has the following advantages:

[0021] 1. This invention, by setting up a tail gas incineration unit, a catalytic oxidation unit, a condensation acid production unit, a tail gas purification unit, and a pyrolysis unit, enables the complete combustion of the Claus unit's tail gas, oxidizing sulfur-containing compounds into SO2. SO2 is then catalytically oxidized to SO3, hydrated, and condensed to produce sulfuric acid. Residual SO2 in the tail gas is converted into sulfuric acid under the action of a low-temperature active catalyst. Acid mist is removed by a high-efficiency demister. The finished sulfuric acid is then fed into a vertical pyrolysis furnace to be pyrolyzed into SO2, which is then mixed with hydrogen sulfide in a specific ratio in the Claus unit to produce sulfur. This invention perfectly combines conventional Claus sulfur production technology with tail gas-to-sulfuric acid technology, solving the problems of substandard Claus tail gas emissions and waste liquid generation. The entire process generates no secondary pollutants from waste liquid, while simultaneously achieving large-scale production.

[0022] 2. This invention sets up a gas guiding component and an expansion and replacement component in the catalytic oxidation unit. The gas guiding component controls the corresponding No. 1 and No. 2 gas bags to contract or expand, blocking or clearing the corresponding passage pipes or connecting pipes, thereby changing the flow direction of the process gas. This facilitates the replacement of the catalyst layer through the expansion and replacement component. Through the above operations, the catalyst can be replaced without stopping the machine. The gas can be guided to other normally operating catalyst layers, ensuring the continuity of production and reducing losses caused by downtime.

[0023] 3. By setting up an unfolding and replacement component, the present invention allows operators to simply open the door panel and automatically remove the catalyst layer from the oxidation reaction chamber by means of the linkage between the connecting rod and the sliding frame. This facilitates maintenance work such as inspection, cleaning, and replacement, ensuring that the oxidation reaction continues to proceed efficiently and avoiding production stagnation or efficiency decline due to untimely maintenance. Attached Figure Description

[0024] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0025] Figure 1 This is a schematic diagram of the overall process of the present invention;

[0026] Figure 2 This is a schematic diagram of the overall structure of the catalytic oxidation unit in this invention;

[0027] Figure 3 This is a schematic diagram of the side profile of the catalytic oxidation unit in this invention;

[0028] Figure 4 This is a schematic diagram of the overall conveying structure of the gas guiding component in this invention;

[0029] Figure 5 Figure 1 is a schematic diagram of the position structure of the gas guide assembly in the present application;

[0030] Figure 6 Figure 2 is a schematic diagram of the structure of the first air bag in the present application;

[0031] Figure 7 Figure 3 is a schematic diagram of the structure of the second air bag in the present application;

[0032] Figure 8 Figure 4 is a schematic diagram of the partial structure of the unfolding replacement assembly in the present application;

[0033] Figure 9 Figure 5 is an exploded schematic diagram of the sliding frame and the blocking frame in the present application;

[0034] Figure 10 Figure 6 is a schematic diagram of the unfolded structure of the oxidation reaction bin after being cut in the present application;

[0035] Figure 11 Figure 7 is a schematic diagram of the structure of the A part in the present application; Figure 5 Figure 8 is an enlarged schematic diagram of the structure of the A part in the present application.

[0036] Figure 1 is a schematic diagram of the position structure of the gas guide assembly in the present application; Figure 2 is a schematic diagram of the structure of the first air bag in the present application; Figure 3 is a schematic diagram of the structure of the second air bag in the present application; Figure 4 is a schematic diagram of the partial structure of the unfolding replacement assembly in the present application; Figure 5 is an exploded schematic diagram of the sliding frame and the blocking frame in the present application; Figure 6 is a schematic diagram of the unfolded structure of the oxidation reaction bin after being cut in the present application; Figure 7 is a schematic diagram of the structure of the A part in the present application; Figure 8 is an enlarged schematic diagram of the structure of the A part in the present application. DETAILED DESCRIPTION

[0037] The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the 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 of the present application. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art without creative labor fall within the scope of protection of the present application.

[0038] Embodiment: as Figures 1-11As shown, the present application provides a technical solution: a system for Claus tail gas recycling, comprising the following steps:

[0039] S1, first make the Claus tail gas into the multi-fuel incinerator in the tail gas incineration unit 1, and become SO2 after incineration, and the high-temperature process gas out of the incinerator enters the waste heat recovery furnace to produce high-pressure saturated steam;

[0040] S2, the process gas after cooling enters the staged SO reactor in the catalytic oxidation unit 2 for catalytic oxidation reaction, and the special PTIL-WXP series catalyst in the reactor oxidizes SO2 gas into SO3, and one or more bed layers are installed in the catalytic oxidation unit according to the change of the content of the raw material components;

[0041] S3, the process gas enters the acid condensing unit 3, and the sulfuric acid vapor in the process gas is condensed into liquid sulfuric acid when heated in the glass tube heat exchanger with air taken from the environment, and flows into the sulfuric acid condensate collection tank under the action of gravity, and then enters the cracking unit 5 after cooling by the heat exchanger;

[0042] S4, the trace SO2 gas in the process gas out of the glass tube condenser enters the tail gas purification unit 4 for removal, and then the process gas enters the high-efficiency mist eliminator to remove SO3 acid mist in the tail gas, and the tail gas realizes ultra-clean emission better than the most stringent emission index;

[0043] S5, the sulfuric acid produced by the acid condensing unit 3 enters the unique vertical cracking furnace in the cracking unit 5, which cracks the sulfuric acid into SO2 gas, and then is sent into the Claus device condenser after being pressurized by the compressor to produce sulfur or is not cooled and enters the Claus furnace as raw material to produce sulfur.

[0044] The furnace temperature of the incinerator in the tail gas incineration unit 1 is controlled at 800-900℃, and the pressure of the incinerator is controlled at micro-negative pressure, at-1-0KPa.

[0045] By controlling the furnace temperature of the incinerator at 800-900℃, the harmful components in the tail gas can be rapidly oxidized at high temperature, completely decomposed and converted into harmless carbon dioxide, sulfur dioxide and other substances, thereby achieving the purpose of efficiently treating tail gas and reducing pollutant emissions.

[0046] The outlet of each catalyst bed in the catalytic oxidation unit 2 is equipped with a high-efficiency finned heat exchanger resistant to high-sulfur medium. By arranging the finned heat exchanger, the fin structure increases the heat exchange area and improves the heat exchange efficiency, so that the reaction heat can be quickly taken away, which helps to maintain the stability of the reaction temperature and ensures the efficient performance of the catalytic oxidation reaction. The finned 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 inlet temperature of the catalyst bed of the reactor is controlled between 380-435℃, the outlet temperature of the reactor is controlled between 270-290℃, and the pressure is controlled at a slight positive pressure.

[0047] By adopting the above technical scheme, the inlet temperature of the catalyst bed of the reactor is controlled between 380-435℃, which provides a suitable active temperature environment for the catalyst. In this temperature range, the catalyst has high activity, which can accelerate the reaction rate, improve the conversion rate and selectivity of the reaction, and make the catalytic oxidation reaction more fully.

[0048] The glass tube heat exchanger in the condensing acid unit 3 is arranged as one or more heat exchange modules according to the raw material, and the glass tube is in the form of a horizontal tube or a vertical tube. A slight negative pressure is maintained on the process gas side of the glass tube condenser 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 glass tube condenser is controlled between 90-110℃.

[0049] By adopting the above technical scheme, by maintaining a slight negative pressure to take away more water, the concentration of sulfuric acid can be accurately controlled, and the outlet temperature of the glass tube condenser is controlled between 90-110℃, which avoids the adverse effects of excessively high or low temperature on the equipment.

[0050] In the PTIL-CC reactor in the tail gas purification unit 4, the gas is oxidized to SO3 under the action of a low-temperature active catalyst, washed with water to become dilute acid, and then enters the condenser for concentration. The temperature in the reactor is controlled below 80℃.

[0051] By adopting the above technical scheme, the low-temperature active catalyst can maintain high activity at a relatively low temperature. Controlling the temperature below 80℃ helps to maintain the optimal activity state of the catalyst, so that the gas can be efficiently oxidized to SO3, improve the conversion rate and selectivity of the reaction, prolong the service life of the catalyst, and reduce the replacement frequency and cost of the catalyst.

[0052] The cracking temperature in the cracking unit 5 is controlled between 900-1000℃, and the sulfuric acid is cracked into SO2 gas, which is cooled to about 300℃ by a waste heat recovery furnace.

[0053] By adopting the above technical scheme, in this temperature range, the sulfuric acid molecules can obtain sufficient energy for the cracking reaction, so that the sulfuric acid is converted into SO2 gas as completely as possible, the utilization rate of raw materials and the production efficiency are improved, and large-scale industrial production is facilitated.

[0054] The device used by a system for recycling Claus tail gas comprises a support 21, three oxidation reaction chambers 22 and four through-chamber pipes 23, the three oxidation reaction chambers 22 are vertically distributed and fixedly installed on the support 21, adjacent oxidation reaction chambers 22 are connected through the through-chamber pipes 23, the transmission of gas between the oxidation reaction chambers 22 is realized, adjacent two through-chamber pipes 23 are connected through the communication pipes 24, the through-chamber pipes 23 and the communication pipes 24 are provided with three gas flow guide assemblies 25 for changing the direction of gas, the oxidation reaction chamber 22 is provided with an unfolding replacement assembly 26 for replacing the catalyst;

[0055] The gas flow guide assembly 25 comprises two symmetrically distributed first isolation frames 2501 and second isolation frames 2502, the first isolation frame 2501 and the second isolation frame 2502 are respectively provided with a first air bag 2503 and a second air bag 2504;

[0056] The unfolding replacement assembly 26 comprises two symmetrically distributed fixed plates 2601, the two fixed plates 2601 are fixedly installed on the inner wall of the oxidation reaction chamber 22, a sliding frame 2602 is slidingly arranged between the two fixed plates 2601, the sliding frame 2602 is provided with a catalyst layer 2603, two symmetrically distributed sliding plates 2606 are slidingly arranged in the oxidation reaction chamber 22, a guide rod 2607 is fixedly arranged between the two sliding plates 2606, two symmetrically distributed connecting rods 2609 are rotatably arranged on the outer wall of the guide rod 2607, and the top end of the two connecting rods 2609 is connected with the sliding frame 2602, and the bottom end is rotatably connected.

[0057] By adopting the above technical scheme, the catalyst layer 2603 can be replaced during the operation of the catalytic oxidation unit 2.

[0058] Two first isolation frames 2501 are located at both ends of the oxidation reaction bin 22 and are fixedly installed on the inner wall of the communication bin pipe 23 between the oxidation reaction bin 22 and the communication pipe 24. A second isolation frame 2502 is fixedly installed on the inner wall of the communication pipe 24. The inner walls of the first isolation frame 2501 and the second isolation frame 2502 are fixedly provided with two symmetrically distributed first baffles 2505 and second baffles 2506, respectively. A side plate 2507 is fixedly arranged on the outer wall of the support 21 near one side of the oxidation reaction bin 22. Two symmetrically distributed pneumatic electromagnetic valves 2508 are fixedly arranged at the top end of the side plate 2507. The first air bag 2503 and the second air bag 2504 are both connected with a gas guide pipe 2509. The other ends of the first air bag 2503 and the second air bag 2504 corresponding to the gas guide pipe 2509 are connected with the gas outlet end of the pneumatic electromagnetic valve 2508. A gas source 2510 is arranged on one side of the support 21. The pneumatic electromagnetic valve 2508 and the gas source 2510 are connected through the gas guide pipe 2509.

[0059] By adopting the above technical scheme, the first air bag 2503 and the second air bag 2504 are expanded or contracted through the cooperation of the electromagnetic valve 2508, the first air bag 2503 and the second air bag 2504, so as to change the process gas flow direction line.

[0060] Two symmetrically distributed transverse plates 2605 are fixedly arranged on the inner wall of the oxidation reaction bin 22. A guide column 2608 corresponding to a guide rod 2607 is fixedly arranged on one side of a sliding plate 2606 close to the transverse plate 2605. The transverse plate 2605 is provided with a guide groove 2614. An arc-shaped groove 2615 is arranged on the side of the transverse plate 2605 away from a connecting rod 2609. The arc-shaped groove 2615 is connected with the guide groove 2614. The guide rod 2607 and the guide column 2608 slide in the arc-shaped groove 2615 and the guide groove 2614.

[0061] A drive shaft 2610 is rotatably arranged at the middle part of one side of the oxidation reaction bin 22 close to the guide column 2608. A universal joint 2611 is fixedly arranged on the inner end of the drive shaft 2610. A lead screw 2612 is fixedly arranged on the other end of the universal joint 2611. A guide block 2613 is threadedly connected on the outer wall of the lead screw 2612. The guide block 2613 is rotatably installed in the middle part of the guide rod 2607.

[0062] Two door plates 2616 are fixedly arranged on the end parts of the two sliding plates 2606 and are used in cooperation with the oxidation reaction bin 22. A sealing strip is arranged at the closed connection between the door plate 2616 and the oxidation reaction bin 22.

[0063] By adopting the above technical scheme, when the door plate 2616 is opened, the sliding frame 2602 can be simultaneously driven to displace, so as to smoothly take out the catalyst layer 2603, thereby reducing the cumbersome operation steps and significantly improving the efficiency of replacing and maintaining the catalyst layer 2603.

[0064] The blocking frame 2604 is arranged above the catalyst layer 2603, and the blocking frame 2604 is fixedly connected with the sliding frame 2602 through bolts.

[0065] By adopting the technical scheme, the blocking frame 2604 is connected with the sliding frame 2602 through bolts, and the blocking frame 2604 limits the catalyst layer 2603, so that the installation and dismounting process is relatively simple and convenient.

[0066] Working principle: as Figure 1 shown, the Claus tail gas enters the unique multi-fuel incinerator of the tail gas incineration unit 1, becomes SO2 after incineration, the incinerator temperature is controlled at 800-900℃, the incinerator pressure is controlled at micro negative pressure, at -1-0KPa, the high-temperature process gas out of the incinerator enters the waste heat recovery furnace to produce high-pressure saturated steam, the process gas after cooling enters the sectional SO2 reactor in the catalytic oxidation unit 2 to carry out catalytic oxidation reaction, under the action of the PTIL-WXP series catalyst, the SO2 gas is oxidized into SO3, the high-efficiency finned heat exchanger resistant to high-sulfur medium is installed at the outlet of each catalyst bed, the reaction heat is taken away through the heat exchange between the high-pressure saturated steam / high-pressure saturated steam water and the process gas, the reactor catalyst bed inlet temperature is controlled at 380-435℃, the reactor outlet temperature is controlled at 270-290℃, the pressure is controlled at micro positive pressure, then the process gas enters the acid condensation unit 3, the sulfuric acid vapor in the process gas is condensed into liquid sulfuric acid in the glass tube heat exchanger when being heat-exchanged with the air taken from the environment, and flows into the sulfuric acid condensate collection tank under the action of gravity, after cooling through the heat exchanger, enters the cracking unit 5, the sulfuric acid condensate enters the unique vertical cracking furnace in the cracking unit 5, the cracking temperature is controlled at 900-1000℃, the sulfuric acid is cracked into SO2 gas, cooled to about 300℃ through the waste heat recovery furnace, and then pressurized through the compressor and sent into the Claus device condenser to produce sulfur or not cooled to enter the Claus furnace as raw material to produce sulfur;

[0067] The trace SO2 gas in the process gas out of the glass tube condenser in the acid condensation unit 2 enters the tail gas purification unit 4 for removal, in the PTIL-CC reactor, the SO2 gas is oxidized into SO3 under the action of the low-temperature active catalyst, becomes dilute acid after water washing, and enters the condenser for concentration, the temperature in the reactor is controlled below 80℃. Then the process gas enters the high-efficiency demister to remove SO3 acid mist in the tail gas, and the tail gas realizes ultra-clean emission better than the most stringent emission index;

[0068] When the PTIL-WXP series catalyst in the catalytic oxidation unit 2 needs to be replaced due to low activity, as Figure 3 , Figure 4As shown, the oxidation reaction bin 22 is provided with three upper, middle and lower, need to replace the catalyst layer 2603 in the oxidation reaction bin 22, first control the gas source 2510 to the required replacement of the oxidation reaction bin 22 in the corresponding pneumatic solenoid valve 2508 to provide input gas, such as Figure 6 、 Figure 7 As shown, the initial state of the first air bag 2503 is the original state, and the second air bag 2504 is in the expanded state. The second air bag 2504 is expanded to block the communication pipe 24. Therefore, the communication pipe 24 is in a closed state in the initial state. After the process gas is cooled, it enters from the bottom of the bin pipe 23, passes through the three oxidation reaction bins 22 in turn, and is discharged from the top of the bin pipe 23 to enter the condensation acid unit 3.

[0069] The first air bag 2503 corresponding pneumatic solenoid valve 2508 is opened, and the second air bag 2504 corresponding pneumatic solenoid valve 2508 is closed at the same time. At this time, the gas input by the gas source 2510 enters the first air bag 2503 through the opened pneumatic solenoid valve 2508 and the gas guide pipe 2509. With the continuous injection of gas, the first air bag 2503 is gradually inflated until it blocks the bin pipe 23 connected to both ends of the corresponding oxidation reaction bin 22, thereby blocking the process gas from entering the oxidation reaction bin 22.

[0070] At the same time, the second air bag 2504 corresponding pneumatic solenoid valve 2508 is closed, and the second air bag 2504 is retracted due to its own elastic force. During the retraction process, the internal space of the second air bag 2504 is reduced, forcing the internal gas to be discharged through the corresponding pneumatic solenoid valve 250 outlet. At this time, the process gas does not pass through the oxidation reaction bin 22, but directly enters the corresponding bin pipe 23 through the communication pipe 24, continuing its subsequent flow process.

[0071] Then, manually rotate the handle on the back of the corresponding oxidation reaction chamber 22. The handle drives the lead screw 2612 to rotate in the forward direction via the drive shaft 2610 and universal coupling 2611. The rotation of the lead screw 2612 drives the slide plate 2606 to move under the guidance of the guide post 2608 and guide groove 2614 through the guide block 2613 and guide rod 2607. The movement of the slide plate 2606 drives the door panel 2616 to move synchronously. After the slide plate 2606 moves to the end limit distance, the guide post 2608 is located at the end of the guide groove 2614, and the guide rod 2607 is located at the connection between the guide groove 2614 and the arc groove 2615. As the lead screw 2612 continues to rotate, the guide block 261... 3. Drive the guide rod 2607 into the arc groove 2615, so that the slide plate 2606 drives the door panel 2616 to flip downward around the guide post 2608. During the movement, the guide rod 2607 pulls the sliding frame 2602 out of the oxidation reaction chamber 22 through the connecting rod 2609. After removing the top bolt of the baffle 2604 with a screwdriver, remove the baffle 2604 and the catalyst layer 2603 in sequence. After replacing the catalyst layer 2603, fix the baffle 2604 and the sliding frame 2602 with bolts to limit the catalyst layer 2603. Then manually turn the handle in the opposite direction to reset the catalyst layer 2603 and the door panel 2616 according to the reverse steps above.

[0072] Finally, open the pneumatic solenoid valve 2508 corresponding to the second airbag 2504, and at the same time close the pneumatic solenoid valve 2508 corresponding to the first airbag 2503. Following the same steps as above, the second airbag 2504 expands and blocks the connecting pipe 24, and the first airbag 2503 returns to its initial state. The process gas can then enter the oxidation reaction chamber 22.

[0073] Obviously, those skilled in the art can make various modifications and variations to this invention without departing from its spirit and scope. Therefore, if these modifications and variations fall within the scope of the claims of this invention and their equivalents, this invention also intends to include these modifications and variations.

Claims

1. A system for Claus tail gas recycle utilization, characterized by: It comprises the following steps: S1, first make the Claus tail gas into the tail gas incineration unit (1) in the multi-fuel incinerator, after incineration into SO2, high temperature process gas out of the incinerator into the waste heat recovery furnace to produce high pressure saturated steam; S2, the process gas after cooling into the catalytic oxidation unit (2) in the staged SO reactor for catalytic oxidation reaction, the reactor in the special PTIL-WXP series catalyst will be SO2 gas oxidation into SO3, according to the change of the content of raw material components installed in the catalytic oxidation unit in one or more bed; S3, the process gas into the condensing acid unit (3), the sulfuric acid vapor in the process gas is condensed into liquid sulfuric acid in the glass tube heat exchanger when the air is exchanged from the environment and flows into the sulfuric acid condensate collection tank under the action of gravity after cooling in the heat exchanger into the cracking unit (5); S4, the trace SO2 gas in the process gas out of the glass tube condenser, into the tail gas purification unit (4) to remove, then the process gas into the high efficiency mist eliminator to remove SO3 acid mist in the tail gas, tail gas to achieve the ultra clean emission under the most stringent emission standards; S5, the sulfuric acid produced by the condensing acid unit (3) into the unique vertical cracking furnace in the cracking unit (5), the sulfuric acid is cracked into SO2 gas, then pressurized by compressor and sent into the Claus device condenser to produce sulfur or not through cooling into the Claus furnace as raw material to produce sulfur.

2. A Claus tail gas regeneration utilization system as claimed in claim 1, characterized in that, The incinerator temperature in the tail gas incineration unit (1) is controlled at 800-900 ℃, and the incinerator pressure is controlled at micro negative pressure, at-1-0 KPa.

3. A Claus tail gas regeneration utilization system as claimed in claim 1, characterized in that, The outlet of each catalyst bed in the catalytic oxidation unit (2) is equipped with high efficiency fin heat exchanger resistant to high sulfur medium, and the fin heat exchanger uses high pressure saturated steam / high pressure saturated steam water to exchange heat with process gas to take away the reaction heat, the inlet temperature of the reactor catalyst bed is controlled at 380-435 ℃, the outlet temperature of the reactor is controlled at 270-290 ℃, and the pressure is controlled at micro positive pressure.

4. The system for Claus tail gas regeneration and utilization of claim 1, wherein, The glass tube heat exchanger in the condensing acid unit (3) is confirmed to be set as one or more heat exchange modules according to the raw material, and the glass tube is in the form of horizontal tube or vertical tube, and the micro negative pressure is maintained on the process gas side of the glass tube condenser to reduce the boiling point of water in the process, take away more water to realize the control of sulfuric acid concentration, and the outlet temperature of the glass tube condenser is controlled at 90-110 ℃.

5. The system for Claus tail gas regeneration and utilization of claim 1, wherein, In the PTIL-CC reactor in the tail gas purification unit (4), the gas is oxidized to SO3 under the action of low temperature active catalyst, washed with water to become dilute acid, and enters the condenser for concentration, and the temperature in the reactor is controlled below 80 ℃.

6. A Claus tail gas regeneration utilization system as claimed in claim 1, characterized in that, The cracking temperature in the cracking unit (5) is controlled at 900-1000 ℃, which cracks the sulfuric acid into SO2 gas, and the temperature is cooled to about 300 ℃ by waste heat recovery furnace.

7. A device for use in a Claus tail gas regeneration system as claimed in any one of claims 1 to 6, characterized in that The device comprises a support (21), three oxidation reaction chambers (22) and four through-chamber pipes (23), the three oxidation reaction chambers (22) are vertically distributed and fixedly installed on the support (21), adjacent oxidation reaction chambers (22) are connected through the through-chamber pipes (23) to realize the transmission of gas among the oxidation reaction chambers (22), and adjacent two through-chamber pipes (23) are connected through a communication pipe (24), the through-chamber pipes (23) and the communication pipe (24) are provided with three gas flow guiding assemblies (25) for changing the direction of gas, and the oxidation reaction chamber (22) is provided with an unfolding replacement assembly (26) for replacing catalysts; The gas flow guiding assembly (25) comprises two symmetrically distributed first isolation frames (2501) and second isolation frames (2502), and the first isolation frame (2501) and the second isolation frame (2502) are respectively provided with a first air bag (2503) and a second air bag (2504); The unfolding replacement assembly (26) comprises two symmetrically distributed fixed plates (2601) fixedly installed on the inner wall of the oxidation reaction chamber (22), a sliding frame (2602) slidably arranged between the two fixed plates (2601), a catalyst layer (2603) arranged in the sliding frame (2602), two symmetrically distributed sliding plates (2606) slidably arranged in the oxidation reaction chamber (22), a guide rod (2607) fixedly arranged between the two sliding plates (2606), and two symmetrically distributed connecting rods (2609) rotatably arranged on the outer wall of the guide rod (2607), and the top ends of the two connecting rods (2609) are rotatably connected with the sliding frame (2602) and the bottom ends are rotatably connected.

8. A Claus tail gas regeneration utilization system and apparatus as claimed in claim 7, characterized in that, The two first isolation frames (2501) are respectively located at both ends of the oxidation reaction chamber (22) and are fixedly installed on the inner wall of the through-chamber pipe (23) between the oxidation reaction chamber (22) and the communication pipe (24), the second isolation frame (2502) is fixedly installed on the inner wall of the communication pipe (24), the inner walls of the first isolation frame (2501) and the second isolation frame (2502) are respectively fixedly provided with two symmetrically distributed first partitions (2505) and second partitions (2506), a side plate (2507) is fixedly arranged on the outer wall of the support (21) close to one side of the oxidation reaction chamber (22), two symmetrically distributed pneumatic electromagnetic valves (2508) are fixedly arranged at the top end of the side plate (2507), the first air bag (2503) and the second air bag (2504) are both provided with a gas guide pipe (2509) penetratingly connected, and the other end of the gas guide pipe (2509) corresponding to the first air bag (2503) and the second air bag (2504) is penetratingly connected with the gas outlet end of the pneumatic electromagnetic valve (2508), and a gas source (2510) is arranged on one side of the support (21), and the pneumatic electromagnetic valve (2508) and the gas source (2510) are penetratingly connected through the gas guide pipe (2509).

9. The Claus tail gas regeneration system and apparatus of claim 7, wherein, Two symmetrical transverse plates (2605) are fixedly arranged on the inner wall of the oxidation reaction bin (22), a guide column (2608) corresponding to a guide rod (2607) is fixedly arranged on one side of a sliding plate (2606) close to the transverse plate (2605), the transverse plate (2605) is provided with a guide groove (2614), an arc-shaped groove (2615) is formed on the side of the transverse plate (2605) away from a connecting rod (2609), the arc-shaped groove (2615) is in through connection with the guide groove (2614), and the guide rod (2607) and the guide column (2608) slide in the arc-shaped groove (2615) and the guide groove (2614); A driving shaft (2610) is rotatably arranged on the middle of one side of the oxidation reaction bin (22) close to the guide column (2608), a universal joint (2611) is fixedly arranged on the inner end of the driving shaft (2610), a screw rod (2612) is fixedly arranged on the other end of the universal joint (2611), a guide block (2613) is in screw connection with the outer wall of the screw rod (2612), and the guide block (2613) is rotatably arranged on the middle of the guide rod (2607); Two end portions of the sliding plate (2606) are fixedly provided with door plates (2616) used in cooperation with the oxidation reaction bin (22), and a sealing strip is arranged at the closed connection position of the door plate (2616) and the oxidation reaction bin (22).

10. The system and the device of Claus tail gas regeneration and utilization according to claim 7, characterized in that, A blocking frame (2604) is arranged above the catalyst layer (2603), and the blocking frame (2604) and the sliding frame (2602) are fixedly connected through bolts.

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