System and process for removing organic sulfur in coke oven gas

Abstract

The invention belongs to the technical field of coke oven gas treatment, and particularly relates to a system and process for removing organic sulfur in coke oven gas, the system comprises an alkaline washing tower, a desulfurization system, a regeneration system, an alkaline liquor storage tank, a sulfur recycling system, a sulfur separation unit and an alkaline liquor circulating pump, the alkaline washing tower is internally provided with a demister, a filler section and a liquid collector in sequence from top to bottom, a coke oven gas inlet and a circulating alkali liquor outlet are formed in the bottom of the alkaline washing tower; through the synergistic effect of an amine liquid composite formula and a three-section type filler, the hydrolysis rate of organic sulfur (COS / CS2) is larger than or equal to 99%, the sulfur recovery rate is larger than or equal to 99.5%, 99% HCN and tar impurities are synchronously removed, a regeneration system adopts a lean and rich liquid heat exchanger to recover heat energy, and steam energy consumption is reduced by 20-30%; the service life of the amine liquid is prolonged by 3 times through an anti-oxidation-corrosion inhibition system, the supplementing cost is reduced, H2S is completely converted into high-purity sulfur (more than or equal to 99.9%) through complex iron catalysis, and sulfur slag pollution is avoided.

Description

Technical Field

[0001] The present invention belongs to the technical field of coke oven gas treatment, and specifically relates to a system and process for removing organic sulfur from coke oven gas. Background Art

[0002] Coke oven gas is generated during the coking process. Generally, 300 - 350 Nm3 of coke oven gas is produced per ton of dry coal. This process involves dry distilling coal in a coke oven in the absence of air to obtain coke, producing a yellowish-brown gas-vapor mixture mainly composed of hydrogen (H2) and methane (CH4). Coke oven gas is an important industrial gas and can be used as fuel. In addition, hydrogen and methane in coke oven gas can be used as reducing agents for iron reduction and can be used to produce chemical products such as nitrogen fertilizers, methanol, dimethyl ether, natural gas, and fuel oil, with relatively high economic value. However, the sulfide content in coke oven gas is relatively high, with H2S being 5 - 7 g / m 3 , CS2 being 300 - 500 mg / m 3 , and COS being 100 - 200 mg / m 3 . If these sulfides are not deeply removed, it will affect the subsequent use of coke oven gas. Coke oven gas also contains 1.5 - 3% of CO2, and in addition, there are relatively high levels of impurities such as tar and naphthalene.

[0003] Coke oven gas desulfurization processes are divided into dry desulfurization and wet desulfurization. Currently, the more widely used one is the catalytic oxidation wet desulfurization process. Dry desulfurization refers to the process of using powdered or granular absorbents or adsorbents such as iron oxide, activated carbon, and hydrolysis catalysts to remove sulfur-containing gases from flue gas. Due to the limited sulfur capacity of the adsorbent, dry desulfurization is suitable for flue gas with relatively low sulfur concentration. In addition, impurities such as tar and naphthalene in coke oven gas will seriously contaminate the catalyst or adsorbent particles, resulting in difficult regeneration and short lifespan. In addition, the pressure drop of the dry method is generally higher than 0.5 kPa, resulting in a 15 - 20% increase in the energy consumption of subsequent use. For example, patent CN118406513A. The catalytic oxidation wet desulfurization process has a good effect on removing H2S, but the organic sulfur removal rate is lower than 60%, and a large amount of by-products such as salts are generated during the treatment process, which not only easily clogs the equipment, but also requires high costs to treat these pollutants, and also causes greater pressure on the environment. For example, patents CN119220306A and CN118421382A. Therefore, the present invention provides a system and process for removing organic sulfur from coke oven gas. Summary of the Invention

[0004] In order to make up for the deficiencies of the prior art and solve at least one technical problem proposed in the background art.

[0005] The technical solution adopted by the present invention to solve its technical problems is as follows: A system for removing organic sulfur from coke oven gas according to the present invention includes an alkali scrubbing tower, a desulfurization system, a regeneration system, an alkali liquid storage tank, a sulfur resource utilization system, a sulfur separation unit, and an alkali liquid circulation pump; in the alkali scrubbing tower, a demister, a packing section, and a liquid collector are sequentially arranged from top to bottom. The top of the alkali scrubbing tower has a circulating alkali liquid inlet and a coke oven gas outlet, and the bottom has a coke oven gas inlet and a circulating alkali liquid outlet; the desulfurization system includes a desulfurization tower, a rich liquid circulation pump, and an amine liquid cooler. In the desulfurization tower, a demister, a packing layer, and a liquid collector are sequentially arranged from top to bottom. The top of the desulfurization tower has a lean amine liquid inlet and a desulfurized coke oven gas outlet, the middle has a circulating amine liquid inlet, and the bottom has a coke oven gas inlet and a rich amine liquid outlet.

[0006] Preferably, the regeneration system includes a regeneration tower, a reboiler, a condensation reflux device, a lean liquid circulation pump, an acid gas cooler, a reflux pump, a rich and lean liquid heat exchanger, and a lean liquid cooler. In the regeneration tower, a condensation reflux section, a multi-stage stripping packing layer, and a high-temperature reboiler section are sequentially arranged from top to bottom. The top of the regeneration tower is provided with a rich amine liquid inlet, an acid gas outlet, and a lean amine liquid reflux port. A steam distributor is arranged in the middle, and the bottom is connected to the reboiler and the lean amine liquid storage tank.

[0007] Preferably, the sulfur resource utilization system includes a composite complex iron tail gas treatment device, which is connected to the top of the regeneration tower and is used for treating the acid gas desorbed from the regeneration tower to convert the sulfur therein into sulfur. The overflow pipe of the regeneration tower is connected to the top of the desulfurization tower to ensure smooth overflow liquid. The composite complex iron tail gas treatment device includes an oxidation reaction tower, a solution circulation pump, and a blower. It includes a solution regeneration tank, a sulfur-rich substance pump, and a sulfur melting kettle.

[0008] Preferably, a filter block is arranged on the coke oven gas inlet at the bottom of the alkali scrubbing tower. A hollow groove is formed inside the filter block. A connecting pipe is communicated with one side of the filter block. The top surface of the hollow groove is rotatably connected with a connecting frame. A filter screen is fixedly connected to the inner wall of the connecting frame. The bottom surface of the filter block is provided with a discharge groove communicated with the hollow groove. The cleaning is arranged on one side of the discharge groove close to the connecting pipe. The bottom surface of the connecting frame fits with the inclined side of the discharge groove. A sealing component for sealing the discharge groove is arranged on the filter block. A push rod is slidably connected to one side of the filter block close to the push rod. The push rod is used to push the connecting frame. A ring is fixedly connected to the surface of the push rod. A first spring is fixedly connected between the ring and the filter block.

[0009] Preferably, an elastic block that fits with the connecting frame is fixedly connected to the inner wall of the hollow groove. The inside of the elastic block is a hollow structure. A connecting groove is formed inside the connecting frame. A group of connecting holes that communicate with each other are formed between the elastic block and the connecting groove. A group of air outlet holes that communicate with the connecting groove are formed on the top surface of the inner wall of the connecting frame.

[0010] Preferably, the sealing assembly includes a sealing plate which is torsionally connected to the bottom surface of the filter block through a torsion spring. The sealing plate is used to seal the discharge chute. A magnetic block is fixedly connected to the top surface of the sealing plate. A chute is formed on the bottom surface of the connection frame, and a magnetic plate which repels the magnetic block is slidably connected to the inner wall of the chute. A fixing plate is fixedly connected to the side of the magnetic plate away from the connecting pipe. A connecting plate is fixedly connected to the side of the connection frame close to the fixing plate, and a second spring is fixedly connected between the connecting plate and the fixing plate.

[0011] A process for removing organic sulfur from coke oven gas. This process uses the above-mentioned system for removing organic sulfur from coke oven gas, and the method includes the following steps:

[0012] S1: Let the sulfur-containing coke oven gas enter the caustic scrubber from the bottom, contact countercurrently with the caustic liquid sprayed from the top, and then be discharged from the top of the tower. The caustic liquid enters the caustic scrubber from the top and is discharged from the bottom, and is continuously circulated in the caustic scrubber and the caustic liquid storage tank through the caustic liquid circulation pump.

[0013] S2: Lean amine liquid is sprayed downward from the top of the tower, fully contacts with the rising coke oven gas, absorbs H2S, COS and CS2 therein, forms rich amine liquid and is discharged from the bottom of the tower. The rich amine liquid is divided into two parts after passing through the rich liquid circulation pump (4), and one part goes to the regeneration system.

[0014] S3: After the rich amine liquid is heated and exchanged in the rich and lean liquid heat exchanger, it enters from the top of the regeneration tower, flows downward through the packing layer, and contacts countercurrently with the rising steam generated by the reboiler at the bottom, and acidic gases such as H2S and CO2 are desorbed. The regenerated lean amine liquid is collected in the tower kettle, and is divided into two parts after being pressurized by the lean liquid circulation pump.

[0015] S4: Part of the acidic gases such as H2S and CO2 are returned to the top of the desulfurization tower for recycling, and the other part is heated by the reboiler to form a steam rising gas source; the desorbed acidic gases are discharged from the top of the tower, cooled by the condenser and then enter the gas-liquid separator, and the separated acidic gases are sent to the sulfur recovery unit.

[0016] S5: The sulfur resource system is used to treat the acidic gas desorbed from the regeneration tower, convert the sulfur therein into sulfur, and all the S in the complex ferric chelate tail gas treatment device is converted into sulfur. The acidic gas enters from the bottom of the oxidation reaction tower and contacts countercurrently with the ferric chelate solution flowing from top to bottom.

[0017] S6: The H2S in the acidic gas is oxidized to elemental sulfur and dissolved in the solution. The desulfurized CO2 gas is discharged from the top of the tower, and the sulfur-rich ferric chelate solution flows out from the bottom of the tower, and enters the sulfur separation unit after passing through the solution circulation pump for sulfur elemental separation and ferric chelate oxidation regeneration.

[0018] The beneficial effects of the present invention are as follows:

[0019] 1. The present invention realizes a hydrolysis rate of organic sulfur (COS / CS2) ≥ 99%, a sulfur recovery rate ≥ 99.5%, synchronously removes 99% of HCN and tar impurities through the synergistic effect of an amine solution composite formula and a three-stage packing. The regeneration system recovers heat energy by using a rich and lean liquid heat exchanger, reducing steam energy consumption by 20 - 30%. The antioxidant - corrosion inhibition system extends the life of the amine solution by 3 times, reduces the supplementary cost, and all H2S is catalytically converted into high-purity sulfur (≥99.9%) through chelated iron, avoiding sulfur residue pollution.

[0020] 2. The online conductivity monitoring of the regeneration tower and the linkage control of the pH / ORP of the sulfur system in the present invention realize full-process automation, with a resistance to flow rate fluctuations of ±20% and an efficiency fluctuation ≤ 2%. The Hastelloy packing in the regeneration tower resists corrosion, and the skimmer in the desulfurization tower removes ≥ 95% of floating oil. The equipment maintenance cycle is extended by 50%, and the modular design reduces the floor area by 30%. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] The present invention will be further described below with reference to the accompanying drawings.

[0022] Figure 1 is the system block diagram in the present invention;

[0023] Figure 2 is the structural schematic diagram of the caustic scrubbing tower and the filter block in the present invention;

[0024] Figure 3 is the internal structural schematic diagram of the filter block in the present invention;

[0025] Figure 4 is Figure 3 the enlarged view at A of

[0026] Figure 5 is Figure 3 the enlarged view at B of

[0027] Figure 6 is the process flow diagram in the present invention.

[0028] In the figure: 1. Caustic scrubbing tower; 2. Caustic liquid circulation pump; 3. Desulfurization tower; 4. Rich liquid circulation pump; 5. Amine liquid cooler; 6. Rich and lean liquid heat exchanger; 7. Regeneration tower; 8. Reboiler; 9. Acid gas cooler; 10. Reflux pump; 11. Lean liquid circulation pump; 12. Lean liquid cooler; 13. Oxidation reaction tower; 14. Solution circulation pump; 15. Sulfur separation unit; 16. Fan; 17. Rich sulfur substance pump; 18. Sulfur melting kettle; 19. Caustic liquid storage tank. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0029] In order to make the technical means, creative features, achieved purposes and effects of the present invention easy to understand, the present invention will be further described below in conjunction with specific embodiments.

[0030] Example 1: AsFigure 1 As shown in the figure, a system for removing organic sulfur from coke oven gas according to an embodiment of the present invention includes an alkali scrubbing tower 1, a desulfurization system, a regeneration system, an alkali liquid storage tank 19, a sulfur resource utilization system, and an alkali liquid circulation pump 2; in the alkali scrubbing tower 1, a demister, a packing section, and a liquid collector are sequentially arranged from top to bottom. The top of the alkali scrubbing tower 1 has a circulating alkali liquid inlet and a coke oven gas outlet, and the bottom has a coke oven gas inlet and a circulating alkali liquid outlet; the desulfurization system includes a desulfurization tower 3, a rich liquid circulation pump 4, and an amine liquid cooler 5. In the desulfurization tower 3, a demister, a packing layer, and a liquid collector are sequentially arranged from top to bottom. The top of the desulfurization tower 3 has a lean amine liquid inlet and a desulfurized coke oven gas outlet, the middle has a circulating amine liquid inlet, and the bottom has a coke oven gas inlet and a rich amine liquid outlet;

[0031] The sulfur-containing coke oven gas enters the alkali scrubbing tower 1 from the bottom and contacts the alkali liquid sprayed from the top in a countercurrent manner. After effectively removing tar, ammonia, and HCN, it is discharged from the top of the tower. The alkali liquid enters the alkali scrubbing tower 1 from the top and is discharged from the bottom, and is continuously circulated in the alkali scrubbing tower 1 and the alkali liquid storage tank 19 through the alkali liquid circulation pump 2. The alkali liquid storage tank 19 is used to store and supply the alkali liquid to ensure the stability of the alkali liquid concentration in the alkali scrubbing tower 1. The alkali liquid circulation pump 2 transports the alkali liquid from the storage tank to the top spraying device of the alkali scrubbing tower 1 to form a uniform spray, improving the contact efficiency between the alkali liquid and the coke oven gas and ensuring the effective removal of impurities. The gas hole tower velocity in the alkali scrubbing tower 1 is 1 - 2 m / s, preferably 1.5 m / s; the height is 5 - 10 m, preferably 7 m; the packing is made of PP material, and the specific surface area is 200 - 300 m 2 / m 3 , preferably 250 m 2 / m 3 ; the spraying density is 10 - 20 m 3 / (m 2 ·h), preferably 15 m 3 / (m 2 ·h). The alkali liquid is one or a mixture of NaOH and Na2CO3, and the pH is 8 - 12, preferably 10;

[0032] The lean amine liquid sprays down from the top of the tower and fully contacts the rising coke oven gas, absorbing H2S, COS, and CS2 therein to form a rich amine liquid that is discharged from the bottom of the tower. The rich amine liquid is divided into two parts after passing through the rich liquid circulation pump 4. One part goes to the regeneration system, and the other part enters the amine liquid cooler 5 and is sprayed from the middle section of the desulfurization tower 3 to maintain the temperature stability in the tower;

[0033] The demister is used to intercept liquid droplets in the gas, prevent amine liquid entrainment, and reduce the amine liquid loss rate. An oil skimmer and a sight glass are arranged in the liquid collector. The oil skimmer is used to remove floating oil in the rich amine liquid, and the sight glass is convenient for observing the liquid level and color changes. The packing layer is a three-stage combined packing layer: the bottom layer is a regular packing, and the specific surface area is 100 - 150 m 2 / m 3, with a filling height of 3 - 5 m, used to enhance the mass transfer and absorption of H2S; the middle layer is modified ceramic Intalox saddles with a nano-metal oxide coating on the surface, and the metal oxide is one or a mixture of two of zinc oxide, nickel oxide, and iron oxide, with a specific surface area of 150 - 200 m 2 / m 3 , with a filling height of 3 - 5 m, promoting the hydrolysis reaction of COS and CS2; the top layer is polypropylene cascade rings, with a specific surface area of 200 - 250 m 2 / m 3 , with a filling height of 3 - 5 m, for deep removal of residual sulfides. A gas-liquid distributor is set at the upper part of each section of the packing: the gas distributor adopts a combined structure of a double-layer perforated plate and a swirl guide vane, with an opening rate of 30 - 40%, ensuring uniform distribution of the coal gas and a pressure drop ≤ 30 Pa; the liquid distributor is composed of an annular main pipe and a double-row radial spray pipe, equipped with hollow conical atomizing nozzles to achieve full coverage of the lean amine liquid;

[0034] The operating pressure in the desulfurization tower 3 is 3 - 10 kPa(G), the operating temperature is controlled at 40 - 50 °C, the lean liquid amine concentration is 30 - 50 wt%, preferably 40 wt%, the gas-liquid ratio is 150 - 300, preferably 250, and the composition of the lean amine liquid is 20 - 40% of methyldiethanolamine, 5 - 10% of diethanolamine, 5 - 10% of ethanolamine, 5 - 10% of tert-butyldiethanolamine, 0.5 - 3% of piperazine, 1 - 3% of butylated hydroxyanisole, 1 - 5% of diethyl thiolcarbamate, and 0.5 - 2% of benzotriazole;

[0035] The main absorption principle is as follows: The alkanolamine molecules of the main absorbent contain active groups such as nitrogen atoms and hydroxyl groups. These groups have strong nucleophilicity and can form chemical bonds with sulfur atoms. For inorganic sulfur, such as hydrogen sulfide (H2S), the alkanolamine molecules can combine with it through an acid-base reaction. As a base, the alkanolamine undergoes a proton transfer with acidic H2S to form a relatively stable amine salt, thereby capturing the inorganic sulfur into the absorbent system. For organic sulfur, taking carbonyl sulfide (COS) as an example, the active groups of the alkanolamine molecules can attack the carbonyl carbon in the COS molecule, undergoing a nucleophilic addition reaction, causing the COS molecule to hydrolyze into CO2 and H2S, achieving deep removal of organic sulfur. Due to the existence of special selective adsorption active sites for COS molecules in its molecular structure, during the process of absorbing sulfur compounds, it can preferentially and deeply remove COS, while having a relatively weak adsorption effect on CO2, thus starting the selective removal process of the two from the source of the absorbent, precisely targeting and adsorbing sulfur elements. At the same time, 1-5% by mass of an antioxidant with strong antioxidant properties is added as an antioxidant, which can efficiently scavenge the free radicals generated during the recycling of the absorbent, prevent the absorbent from oxidizing and deteriorating, and ensure the chemical structure stability of the main absorbent; 1-5% of a corrosion inhibitor that can effectively inhibit metal corrosion is added. It can form a dense protective film on the contact surface between the absorbent and the equipment, effectively avoiding equipment corrosion, extending the service life of the equipment, and ensuring the stable and efficient operation of the entire desulfurization system. The two work together organically to build a solid and efficient "composite protection system".

[0036] The regeneration system includes a regeneration tower 7, a reboiler 8, a condensation reflux device, a lean liquid circulation pump 11, an acid gas cooler 9, a reflux pump 10, a rich-lean liquid heat exchanger 6, and a lean liquid cooler 12. In the regeneration tower 7, a condensation reflux section, a multi-stage stripping packing layer, and a high-temperature reboiling section are sequentially arranged from top to bottom. The top of the regeneration tower 7 is provided with a rich amine liquid inlet, an acid gas outlet, and a lean amine liquid reflux port. A steam distributor is configured in the middle, and the bottom is connected to the reboiler 8 and a lean amine liquid storage tank;

[0037] The rich amine liquid is heat-exchanged by the rich-lean liquid heat exchanger 6 and then enters from the top of the regeneration tower 7. It flows downward through the packing layer and countercurrently contacts the rising steam generated by the reboiler 8 at the bottom, stripping out acidic gases such as H2S and CO2. The regenerated lean amine liquid collects in the tower bottom and is pressurized by the lean liquid circulation pump 11 and then divided into two parts. One part is cooled to 35-45°C through the rich-lean liquid heat exchanger 6 and the lean liquid cooler 12 and then returns to the top of the desulfurization tower 3 for recycling. The other part is heated by the reboiler 8 to form a rising steam gas source; the stripped acidic gases are discharged from the top of the tower, cooled by the condenser and then enter the gas-liquid separator. The separated acidic gases are sent to the sulfur recovery unit, and the condensate returns to the top of the regeneration tower 7 through the reflux pump 10 to maintain the system water balance;

[0038] The condensation reflux section is internally equipped with an efficient wire mesh demister and condensation coils. The porosity of the demister is ≥95%, intercepting the amine liquid droplets entrained in the gas phase, and the amine liquid loss rate is ≤0.1%. The condensation coils are fed with circulating cooling water (temperature ≤30°C), and part of the rising steam is condensed and then returned to the top of the tower by the reflux pump 10. The stripping packing layer is divided into a three-stage enhanced stripping structure: the top layer uses stainless steel structured packing (specific surface area 80 - 120 m 2 / m 3 , packing height 3 - 7 m), with the surface coated with an alumina-titania composite catalyst (loading 2 - 10%), promoting the rapid desorption of H2S; the middle layer is filled with surface-modified honeycomb ceramic packing (specific surface area 150 - 180 m 2 / m 3 , packing height 3 - 7 m); the bottom layer is provided with dumped metal Pall rings (specific surface area 50 - 80 m 2 / m 3 , packing height 2 - 3 m), made of Hastelloy C276, resistant to the regeneration temperature (120 - 140°C) and acidic environment. The steam distributor is located in the middle of the regeneration tower 7, adopting a combined structure of an annular steam pipe and radial nozzles, with a nozzle aperture of 4 - 6 mm and a steam flow rate of 15 - 20 m / s, ensuring that the steam generated by the reboiler 8 rises evenly and contacts the rich amine liquid countercurrently. The high-temperature reboiler section is provided with a reboiler 8 at the bottom of the tower (the heat source is 0.6 - 1.0 MPa saturated steam), with U-shaped heat exchange tubes inside, maintaining the bottom temperature of the tower at 110 - 130°C; a lean amine liquid storage tank is connected below the reboiler 8, and multi-stage diversion baffles and temperature monitoring thermocouples (accuracy ±0.5°C) are arranged inside the tank to ensure that the residence time of the lean amine liquid is ≥10 minutes and the temperature fluctuation is ≤2°C. At the same time, a liquid distribution system is set up: a bidirectional spiral spray pipe is configured at the rich amine liquid inlet, with a spray density of 8 - 12 m 3 / (m 2 ·h), covering an area of the packing layer ≥98%; the lean amine liquid reflux port adopts a V-shaped groove type liquid distributor, with a groove width of 100 - 150 mm and an opening rate of 25 - 35%, realizing the uniform distribution of the lean amine liquid and the rising steam;

[0039] The operating pressure of the regeneration tower 7 is 80 to 150 kPa(G), preferably 100 kPa(G), the operating temperature is controlled at 105 - 130°C, preferably 120°C, the mass ratio of steam to rich amine liquid is 0.15 - 0.35, preferably 0.25. An on-line conductivity monitor (≤500 μS / cm) and an automatic regeneration device for thermal stable salts (HSS) are provided at the bottom of the regeneration tower 77 to maintain the amine liquid loss rate ≤0.5% / month;

[0040] The sulfur resource utilization system includes a composite complex iron tail gas treatment device, which is connected to the top of the regeneration tower 7 and is used to treat the acid gas desorbed from the regeneration tower 7, converting the sulfur therein into sulfur. The overflow pipe of the regeneration tower 7 is connected to the top of the desulfurization tower 3 to ensure smooth overflow liquid. The composite complex iron tail gas treatment device includes an oxidation reaction tower 13, a solution circulation pump 14 and a fan 16. The sulfur separation unit 15 includes a solution regeneration tank, a sulfur-rich substance pump 17 and a sulfur melting kettle 18;

[0041] The acid gas desorbed from the regeneration tower 7 enters the composite complex iron tail gas treatment device for treatment. Since all organic sulfur has been converted into hydrogen sulfide during the absorption process, all S can be converted into sulfur in the composite complex iron tail gas treatment device, realizing the resource utilization of S. The acid gas enters from the bottom of the oxidation reaction tower 13 and contacts the complex iron solution flowing from top to bottom in a countercurrent manner. The H2S in the acid gas is oxidized to elemental sulfur and dissolved in the solution. After desulfurization, the CO2 gas is discharged from the top of the tower, and the sulfur-rich complex iron solution flows out from the bottom of the tower, enters the sulfur separation unit 15 after passing through the solution circulation pump 14, and undergoes sulfur elemental separation and complex iron oxidation regeneration;

[0042] The pH value of the solution in the oxidation reaction tower 13 is 8.0 - 9.5, preferably 8.8, and is regulated by the linkage of an on-line pH meter and a Na2CO3 automatic dosing system; the oxidation-reduction potential (ORP) is +150 to +250 mV, preferably +200 mV, and is jointly controlled by the dissolved oxygen concentration (3 - 5 ppm) and the Fe3+ / Fe2+ molar ratio (5:1 - 10:1). The sulfur separation unit 15 has a solution regeneration tank and a sulfur melting kettle 18. The sulfur-rich complex iron solution is regenerated with Fe 3+ active components in the solution regeneration tank through air bubbling oxidation (gas-liquid ratio 1:50 - 1:100), while supplementing fresh complexing agent (EDTA 0.2 - 0.5 wt%), FeSO4 (0.3 - 0.8 wt%) and stabilizer (sodium citrate 1 - 3 wt%). The sulfur foam at the top of the regeneration tank is separated and enters the sulfur melting kettle 18, where it is heated to 120 - 130 °C by steam. After the sulfur melts, it is separated by a centrifuge (rotation speed 2000 - 3000 rpm) to prepare sulfur.

[0043] The temperature of the coke oven gas is 40 °C, the pressure is atmospheric pressure, and the composition is 3000 ppm of H2S, 800 ppm of COS, 200 ppm of CS2, 500 ppm of HCN, and 50 mg / Nm of tar 3 3% of CO2. First, the coke oven gas is introduced into the pretreatment tower. The pH of the alkali solution in the pretreatment tower is 8, the spraying density is 10 m 3 / (m 2 ·h), and the specific surface area of the packing is 200 m 2 / m 3After pre-treatment to remove impurities such as HCN and tar, it enters the bottom of the desulfurization tower 3 and contacts countercurrently with the sprayed desulfurization liquid to remove H2S and organic sulfur, and then is discharged from the top of the tower to obtain desulfurized purified gas. The lean amine liquid concentration in the desulfurization tower 3 is 30 wt%, the gas-liquid ratio is 150, and the rich amine liquid absorbed with sulfide enters the tower for regeneration from the top of the regeneration tower 7 after heat exchange. The operating temperature of the regeneration tower 7 is 105 °C, and the steam mass ratio is 0.15. The regenerated acid gas enters the sulfur resource utilization system after condensation, where the pH of the oxidation reaction tower 13 is 8.0, the ORP is +150 mV, and Fe 3+ / Fe 2+ = 5:1;

[0044] The treatment results are as follows: in the desulfurized coal gas, H2S ≤ 10 ppm, COS ≤ 30 ppm, CS2 ≤ 10 ppm, HCN ≤ 5 ppm, and tar ≤ 5 mg / Nm 3 ; among them, the removal rate of HCN is 98.5%, and the removal rate of organic sulfur is 96.2%. The purity of the recovered sulfur is 98.7%. The amine liquid loss rate is 0.5% / month. The detection methods used are: H2S / COS / CS2: gas chromatography (GB / T 11060); HCN: spectrophotometry (HJ / T 28-1999); sulfur purity: subtraction method (GB 2449);

[0045] In the present invention, the deep removal of organic sulfur: through amine liquid hydrolysis + three-stage packing directional conversion, the efficient removal of COS / CS2 is realized, and at the same time, the removal rate of CO2 is reduced to achieve the high-selectivity removal of COS / CO2. The amine liquid is stable in long cycle: the pre-treatment process removes impurities such as tar and benzene, and at the same time, the composite protection system (anti-oxidation + corrosion inhibition) prolongs the life of the amine liquid and reduces the operating cost. High-purity sulfur recovery: first hydrolyze organic sulfur into H2S, and then combine the complex iron-catalyzed oxidation with the molten sulfur centrifugation process, and the sulfur recovery rate ≥ 99.5%.

[0046] Example 2: Compared with Example 1, another implementation mode of the present invention is as follows: for coke oven gas with initial conditions of temperature 50 °C, pressure 5 kPa (G), H2S 5000 ppm, COS 1200 ppm, CS2 400 ppm, HCN 800 ppm, tar 80 mg / Nm 3 and CO2 4%, first pass it through the pre-treatment tower, and use an alkali solution with pH = 10 at a spraying density of 15 m 3 / (m 2 ·h) and a packing layer with a specific surface area of 250 m 2 / m 3 for pre-treatment, effectively removing tar and more than 99% of HCN;

[0047] Subsequently, the coal gas enters the bottom of the desulfurization tower 3 and countercurrently contacts with lean amine solution with a concentration of 40 wt% at a gas-liquid ratio of 250, and the deep removal of H2S and organic sulfur is achieved through a three-stage combined packing (structured packing + modified ceramics + polypropylene cascade ring). The rich amine solution enters the regeneration tower 7 after heat exchange and is regenerated at an operating temperature of 120 °C and a steam mass ratio of 0.25. The acid gas released is introduced into the sulfur resource recovery system and is converted into sulfur in the oxidation reaction tower 13 with pH = 8.8, ORP = +200 mV, and Fe 3+ / Fe 2+ = 7:1;

[0048] In the treated desulfurized coal gas, H2S ≤ 5 ppm, COS ≤ 10 ppm, CS2 ≤ 5 ppm, HCN ≤ 3 ppm, and tar ≤ 3 mg / Nm 3 , the sulfur purity reaches 99.5% (by the difference method, GB2449), the HCN removal rate is 99.3% (by spectrophotometry, HJ / T28-1999), the organic sulfur removal rate is 99.1% (by gas chromatography, GB / T11060.8), and the amine solution loss rate is only 0.3% / month;

[0049] The control test shows that the COS residue in the traditional process without using nano-metal oxide packing reaches 60 ppm, while in the present invention, the desulfurization efficiency is increased to over 99% through the synergistic effect of the packing, the steam energy consumption is reduced by 28%, and the equipment corrosion rate is reduced by 70%, significantly optimizing the comprehensive economy.

[0050] Example 3: Compared with Example 2, another implementation mode of the present invention is as follows: For high-sulfur-load coke oven gas (temperature 60 °C, pressure 10 kPa(G), H2S 8000 ppm, COS 2000 ppm, CS2 600 ppm, HCN 1000 ppm, tar 120 mg / Nm 3 , and CO2 5%), the pretreatment tower uses alkali solution with pH = 12, a spraying density of 20 m 3 / (m 2 ·h) and a packing layer with a specific surface area of 300 m 2 / m 3 ;

[0051] After removing 99% of HCN and tar, the coal gas enters the desulfurization tower 3 and countercurrently contacts with 50 wt% lean amine solution at a gas-liquid ratio of 300, and the deep conversion of H2S and organic sulfur is completed through a three-stage packing layer. The rich amine solution is regenerated in the regeneration tower 7 at 130 °C with a steam mass ratio of 0.35. The acid gas then generates sulfur in the oxidation reaction tower 13 with pH = 9.5, ORP = +250 mV, and Fe 3+ / Fe 2+ = 10:1;

[0052] After treatment, the H2S content in the gas is ≤ 8 ppm, COS ≤ 15 ppm, CS2 ≤ 8 ppm, HCN ≤ 8 ppm, and tar ≤ 8 mg / Nm 3 , the sulfur purity is 99.2% (by the difference method), the organic sulfur removal rate is 98.8% (by gas chromatography), and the amine liquid loss rate is 0.4% / month;

[0053] For the control group equipment without corrosion inhibitor added, the corrosion rate reaches 0.15 mm / year (by the weight loss method, ASTM G31). However, with the benzotriazole corrosion inhibition system in the present invention, the corrosion rate is controlled within 0.05 mm / year, and the sulfur purity remains ≥ 99% under high sulfur load. The steam energy consumption is only 72% of the traditional process, verifying the strong anti-fluctuation and long-term stability of the process.

[0054] Example 4: Compared with Example 3, another implementation mode of the present invention is as follows: Taking typical coke oven gas (temperature 65°C, pressure 8 kPa(G), H2S 6000 ppm, COS 1500 ppm, CS2 500 ppm, HCN 900 ppm, tar 100 mg / Nm 3 , CO2 4.5%) as the treatment object, the pretreatment tower uses an alkaline solution with pH = 10 and a spraying density of 15 m 3 / (m 2 ·h), in combination with a packing layer of 250 m 2 / m 3 to remove tar and 99.5% of HCN;

[0055] In the desulfurization tower 3, 40 wt% amine liquid (methyldiethanolamine + 8% piperazine) contacts the gas countercurrently at a gas-liquid ratio of 250, and COS / CS2 is converted into H2S and deeply removed through the catalytic hydrolysis layer. The regeneration tower 7 analyzes the acidic gas at 120°C and a steam mass ratio of 0.25. Subsequently, the sulfur resource recovery system generates sulfur under the conditions of pH = 8.8, ORP + 200 mV, and Fe 3+ / Fe 2+ = 7:1;

[0056] After treatment, the H2S content in the gas is ≤ 2 ppm, COS ≤ 5 ppm, CS2 ≤ 2 ppm, HCN ≤ 2 ppm, and tar ≤ 2 mg / Nm 3 , the sulfur purity is 99.8% (by the difference method), the organic sulfur removal rate is 99.6% (by gas chromatography), and the amine liquid loss rate is 0.2% / month.

[0057] Example 5: Compared with Example 4, another implementation mode of the present invention is as follows: (1) Using the traditional MDEA process to treat the initial conditions of temperature 50°C, H2S 3000 ppm, COS 800 ppm, CS2 200 ppm, HCN 500 ppm, tar 50 mg / Nm 3, when the coke oven gas contains 23% CO2, the pretreatment tower operates with an alkaline solution at pH = 9 and a spraying density of 8 m 3 / (m 2 ·h), and the specific surface area of the packing is only 150 m 2 / m 3 , resulting in an HCN removal rate of only 89.7%;

[0058] In desulfurization tower 3, a 30 wt% single MDEA solution operates at a gas-liquid ratio of 200. In regeneration tower 7, at 120 °C and a steam mass ratio of 0.38, the liquid loss rate is as high as 1.5% per month. The residual H2S is 11 ppm, and the COS removal rate is 31.3% (gas chromatography method). The amine liquid loss rate is as high as 1.5% per month. Compared with the preferred embodiment of the present invention, the steam energy consumption of the traditional process increases by 50%, the equipment corrosion rate increases by 3 times, and the tar residue reaches 20 mg / Nm 3 , fully demonstrating the comprehensive advantages of the present invention in deep desulfurization, resource recovery, and operation and maintenance costs.

[0059] Index Example 4 (preferred) Example 5 (traditional) <![CDATA[H2S removal rate]]> 99.97％ 98.3％ COS removal rate 99.7％ 81.3％ Amine solution loss rate 0.2% / month 1.5% / month Steam energy consumption 28% reduction Reference value

[0060] Through parameter optimization and process coordination, the present invention is significantly superior to the traditional process within a wide operating range. The preferred embodiment achieves efficient, energy-saving, and low-loss deep desulfurization and resource utilization of organic sulfur.

[0061] Example Six: As Figures 2 to 5 shown, compared with Example One, another embodiment of the present invention is as follows: A filter block 20 is provided at the coke oven gas inlet at the bottom of the alkali washing tower 1. A hollow groove 22 is formed in the filter block 20. A connecting pipe 21 is communicated with one side of the filter block 20. The top surface of the hollow groove 22 is rotatably connected with a connecting frame 24. A filter net 23 is fixedly connected to the inner wall of the connecting frame 24. A discharge groove 27 communicated with the hollow groove 22 is formed in the bottom surface of the filter block 20. The cleaning is arranged on one side of the discharge groove 27 close to the connecting pipe 21. The bottom surface of the connecting frame 24 fits with the inclined side of the discharge groove 27. A sealing component for sealing the discharge groove 27 is arranged on the filter block 20. A push rod 25 is slidably connected to one side of the filter block 20 close to the push rod 25. The push rod 25 is used to push the connecting frame 24. A ring 26 is fixedly connected to the surface of the push rod 25. A first spring is fixedly connected between the ring 26 and the filter block 20;

[0062] Since the coke oven gas contains particulate impurities, these impurities will be removed by the alkali solution sprayed on the top of the alkali washing tower 1, but larger particulate impurities are likely to remain in the alkali washing tower 1. The coke oven gas in this application can be injected into the hollow groove 22 from the connecting pipe 21. At this time, the large particulate impurities in the coke oven gas will be filtered by the filter 23, and then enter the alkali washing tower 1 to improve the effect of subsequent treatment of the coke oven gas. When there are many impurities on the filter 23, the push rod 25 can be moved back and forth, so that the push rod 25 pushes the connecting frame 24 back and forth, so that the connecting frame 24 swings, and then drives the filter 23 to swing, so that the impurities on the filter 23 fall off, and prevent the impurities from accumulating too much on the filter 23, causing the mesh of the filter 23 to be blocked. The impurities will be discharged from the discharge trough 27, and the discharge trough 27 will be sealed with the help of a sealing mechanism after the impurities are discharged.

[0063] An elastic block 34 that fits with the connecting frame 24 is fixedly connected to the inner wall of the hollow groove 22. The interior of the elastic block 34 is a hollow structure. A connecting groove 35 is provided in the connecting frame 24. A group of connecting holes that are connected to the elastic block 34 and the connecting groove 35 are provided. A group of air outlet holes 36 that are connected to the connecting groove 35 are provided on the top surface of the inner wall of the connecting frame 24. When the connecting frame 24 swings, the connecting frame 24 squeezes the elastic block 34, so that the gas in the elastic block 34 enters the connecting groove 35 from the connecting holes, and then blows onto the filter screen 23 from the air outlet holes 36 to blow away impurities on the filter screen 23, thereby improving the cleaning effect of the filter screen 23.

[0064] The sealing assembly includes a sealing plate 33, which is twisted with the bottom surface of the filter block 20 through a torsion spring. The sealing plate 33 is used to seal the discharge trough 27. The top surface of the sealing plate 33 is fixedly connected with a magnetic block 32. The bottom surface of the connecting frame 24 is provided with a slide groove 30. The inner wall of the slide groove 30 is slidably connected with a magnetic plate 31 that repels the magnetic block 32. The side of the magnetic plate 31 away from the connecting pipe 21 is fixedly connected with a fixed plate 28. The side of the connecting frame 24 close to the fixed plate 28 is fixedly connected with a connecting plate 29. The connecting plate 29 is fixedly connected to the fixed plate 28. The connecting frame 24 is fixedly connected with a second spring; when the connecting frame 24 in the present application swings, the bottom surface of the connecting frame 24 will move away from the inclined surface of the discharge chute 27. At this time, the second spring will push the connecting plate 29, so that the magnetic plate 31 driven by the connecting plate 29 moves downward and approaches the magnetic block 32. After the impurities fall from the filter screen 23, the rotation angle of the connecting frame 24 can be controlled so that the magnetic plate 31 is located above the magnetic block 32. At this time, the magnetic block 32 will drive the sealing plate 33 to rotate due to the repulsive force with the magnetic plate 31, so that the sealing plate 33 no longer seals the discharge chute 27, so that the impurities can be discharged from the discharge chute 27.

[0065] like Figure 6As shown in the figure, a process for removing organic sulfur from coke oven gas is provided. This process uses the above-mentioned system for removing organic sulfur from coke oven gas, and the method includes the following steps:

[0066] S1: Let the sulfur-containing coke oven gas enter the caustic scrubber 1 from the bottom, flow countercurrently with the caustic liquor sprayed from the top, and then be discharged from the top of the tower. The caustic liquor enters the caustic scrubber 1 from the top and is discharged from the bottom, and is continuously circulated between the caustic scrubber 1 and the caustic liquor storage tank 19 by the caustic liquor circulation pump 2;

[0067] S2: The lean amine solution is sprayed downward from the top of the tower, comes into full contact with the rising coke oven gas, absorbs H2S, COS and CS2 therein, forms a rich amine solution and is discharged from the bottom of the tower. The rich amine solution is divided into two parts after passing through the rich liquor circulation pump 4, and a part goes to the regeneration system;

[0068] S3: After the rich amine solution is heated by the rich and lean liquor heat exchanger 6, it enters from the top of the regeneration tower 7, flows downward through the packing layer, and contacts countercurrently with the rising steam generated by the bottom reboiler 8, and acidic gases such as H2S and CO2 are desorbed. The regenerated lean amine solution is collected in the tower bottom, and is divided into two parts after being pressurized by the lean liquor circulation pump 11;

[0069] S4: A part of the acidic gases such as H2S and CO2 is returned to the top of the desulfurization tower 3 for recycling, and the other part is heated by the reboiler 8 to form a steam rising gas source; the desorbed acidic gas is discharged from the top of the tower, cooled by the condenser and then enters the gas-liquid separator, and the separated acidic gas is sent to the sulfur recovery unit;

[0070] S5: The sulfur resource system is used to treat the acidic gas desorbed from the regeneration tower 7, convert the sulfur therein into sulfur, and all the S in the composite complex iron tail gas treatment device is converted into sulfur. The acidic gas enters from the bottom of the oxidation reaction tower 13 and contacts countercurrently with the complex iron solution flowing from top to bottom;

[0071] S6: The H2S in the acidic gas is oxidized to elemental sulfur and dissolved in the solution. The desulfurized CO2 gas is discharged from the top of the tower. The sulfur-rich complex iron solution flows out from the bottom of the tower, enters the sulfur separation unit 15 after passing through the solution circulation pump 14, and performs sulfur elemental separation and complex iron oxidation regeneration.

[0072] Working principle: Through amine hydrolysis + three-stage packing directional conversion, the efficient removal of COS / CS2 is realized, and at the same time, the removal rate of CO2 is reduced to achieve high selectivity for COS / CO2 removal. The amine solution is stable for a long period: The pretreatment process removes impurities such as tar and benzene, and at the same time, the composite protection system (anti-oxidation + corrosion inhibition) extends the life of the amine solution and reduces the operating cost. High-purity sulfur recovery: First, the organic sulfur is hydrolyzed to H2S, and then combined with the complex iron catalytic oxidation and sulfur melting centrifugation process, and the sulfur recovery rate is ≥99.5%;

[0073] Coke oven gas can be injected into the hollow groove 22 from the connecting pipe 21. At this time, large particles of impurities in the coke oven gas will be filtered by the filter 23, and then enter the alkali washing tower 1 to improve the effect of subsequent treatment of the coke oven gas. When there are many impurities on the filter 23, the push rod 25 can be moved back and forth so that the push rod 25 pushes the connecting frame 24 back and forth, thereby allowing the connecting frame 24 to swing, and then driving the filter 23 to swing, so that the impurities on the filter 23 fall off, preventing impurities from accumulating too much on the filter 23 and causing the mesh of the filter 23 to be blocked. The impurities will be discharged from the discharge trough 27, and the discharge trough 27 will be sealed with the help of a sealing mechanism after the impurities are discharged; when the connecting frame 24 swings, the connecting frame 24 squeezes the elastic block 34, so that the gas in the elastic block 34 enters the connecting groove 35 from the connecting hole, and then blows onto the filter 23 from the air outlet 36 to blow away the impurities on the filter 23, thereby improving the cleaning effect of the filter 23; when the connecting frame 24 swings, the bottom surface of the connecting frame 24 will be away from the inclined surface of the discharge trough 27, and at this time the second spring will push the connecting plate 29, so that the magnetic plate 31 driven by the connecting plate 29 moves downward and approaches the magnetic block 32, after the impurities fall from the filter 23, the rotation angle of the connecting frame 24 can be controlled so that the magnetic plate 31 is located above the magnetic block 32, and at this time the magnetic block 32 will drive the sealing plate 33 to rotate due to the repulsive force with the magnetic plate 31, so that the sealing plate 33 no longer seals the discharge trough 27, so that the impurities can be discharged from the discharge trough 27.

[0074] The above-mentioned front, back, left, right, top and bottom are all based on the figures in the specification. Figure 1 As a benchmark, according to the person's observation perspective, the side of the device facing the observer is defined as the front, the left side of the observer is defined as the left, and so on.

[0075] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the scope of protection of the present invention.

[0076] The above shows and describes the basic principles, main features and advantages of the present invention. It should be understood by those skilled in the art that the present invention is not limited to the above embodiments. The above embodiments and descriptions are only for explaining the principles of the present invention. Without departing from the spirit and scope of the present invention, the present invention may have various changes and improvements, which fall within the scope of the present invention. The scope of protection of the present invention is defined by the attached claims and their equivalents.

Claims

1. A system for removing organic sulfur from coke oven gas, comprising an alkali scrubber (1), a desulfurization system, a regeneration system, an alkali liquid storage tank (19), a sulfur resource recovery system, a sulfur separation unit (15) and an alkali liquid circulation pump (2); Features: The alkali washing tower (1) is provided with a demister, a packing section and a liquid collector in order from top to bottom. The top of the alkali washing tower (1) is provided with a circulating alkali liquid inlet and a coke oven gas outlet, and the bottom is provided with a coke oven gas inlet and a circulating alkali liquid outlet. The desulfurization system comprises a desulfurization tower (3), a rich liquid circulation pump (4), and an amine liquid cooler (5). The desulfurization tower (3) is provided with a defoamer, a packing layer, and a liquid collector in sequence from top to bottom. The desulfurization tower (3) has a lean amine liquid inlet and a desulfurized coke oven gas outlet at the top, a circulating amine liquid inlet in the middle, and a coke oven gas inlet and a rich amine liquid outlet at the bottom.

2. A system for removing organic sulfur from coke oven gas according to claim 1, characterized in that: The regeneration system comprises a regeneration tower (7), a reboiler (8), a condensation reflux device, a lean liquid circulation pump (11), an acid gas cooler (9), a reflux pump (10), a lean-rich liquid heat exchanger (6) and a lean liquid cooler (12). The regeneration tower (7) is provided with a condensation reflux section, a multi-stage analytical packing layer and a high-temperature reboiling section from top to bottom. The top of the regeneration tower (7) is provided with a rich amine liquid inlet, an acid gas outlet and a lean amine liquid reflux port, a steam distributor is arranged in the middle, and the bottom is connected to the reboiler (8) and a lean amine liquid storage tank.

3. A system for removing organic sulfur from coke oven gas according to claim 2, characterized in that: The sulfur resource recovery system comprises a composite complex iron tail gas treatment device, which is connected to the top of the regeneration tower (7) and is used to treat the acid gas desorbed by the regeneration tower (7) to convert the sulfur therein into sulfur. The overflow pipe of the regeneration tower (7) is connected to the top of the desulfurization tower (3) to ensure smooth overflow liquid. The composite complex iron tail gas treatment device comprises an oxidation reaction tower (13), a solution circulation pump (14) and a fan (16). The sulfur separation unit (15) comprises a solution regeneration tank, a sulfur-rich material pump (17) and a sulfur melting kettle (18).

4. A system for removing organic sulfur from coke oven gas according to claim 3, characterized in that: A filter block (20) is arranged on the coke oven gas inlet at the bottom of the alkali washing tower (1), a hollow groove (22) is provided in the filter block (20), one side of the filter block (20) is connected with a connecting pipe (21), the top surface of the hollow groove (22) is rotatably connected with a connecting frame (24), the inner wall of the connecting frame (24) is fixedly connected with a filter net (23), the bottom surface of the filter block (20) is provided with a discharge groove (27) connected with the hollow groove (22), the discharge groove (27) is close to the connecting pipe (21) is cleaned on one side, the bottom surface of the connecting frame (24) is in contact with the inclined side of the discharge trough (27), a sealing assembly for sealing the discharge trough (27) is provided on the filter block (20), a push rod (25) is slidably connected to the side of the filter block (20) close to the push rod (25), the push rod (25) is used to push the connecting frame (24), a circular ring (26) is fixedly connected to the surface of the push rod (25), and a first spring is fixedly connected between the circular ring (26) and the filter block (20).

5. A system for removing organic sulfur from coke oven gas according to claim 4, characterized in that: An elastic block (34) that fits the connecting frame (24) is fixedly connected to the inner wall of the hollow groove (22); the interior of the elastic block (34) is a hollow structure; a connecting groove (35) is provided in the connecting frame (24); a group of connecting holes that are connected to the elastic block (34) and the connecting groove (35) are provided; and a group of air outlet holes (36) that are connected to the connecting groove (35) are provided on the top surface of the inner wall of the connecting frame (24).

6. A system for removing organic sulfur from coke oven gas according to claim 5, characterized in that: The sealing assembly comprises a sealing plate (33), the sealing plate (33) being twistedly connected to the bottom surface of the filter block (20) through a torsion spring, the sealing plate (33) being used to seal the discharge trough (27), the top surface of the sealing plate (33) being fixedly connected to a magnetic block (32), the bottom surface of the connecting frame (24) being provided with a slide groove (30), the inner wall of the slide groove (30) being slidably connected to a magnetic plate (31) that repels the magnetic block (32), the side of the magnetic plate (31) away from the connecting pipe (21) being fixedly connected to a fixed plate (28), the side of the connecting frame (24) close to the fixed plate (28) being fixedly connected to a connecting plate (29), and a second spring being fixedly connected between the connecting plate (29) and the fixed plate (28).

7. A process for removing organic sulfur from coke oven gas, the process using a system for removing organic sulfur from coke oven gas as claimed in claim 6, characterized in that: The method comprises the following steps: S1: allowing the sulfur-containing coke oven gas to enter the alkali washing tower (1) from the bottom, and then be discharged from the top of the tower after countercurrent contact with the alkali solution sprayed from the top; the alkali solution enters the alkali washing tower (1) from the top and is discharged from the bottom, and is continuously circulated in the alkali washing tower (1) and the alkali solution storage tank (19) through the alkali solution circulation pump (2); S2: Lean amine liquid sprays down from the top of the tower, fully contacts with the rising coke oven gas, absorbs H2S, COS and CS2 therein, forms rich amine liquid and is discharged from the bottom of the tower. The rich amine liquid is divided into two parts after passing through the rich liquid circulation pump (4), and one part goes to the regeneration system; S3: After heat exchange in the rich-lean-liquid heat exchanger (6), the rich amine liquid enters from the top of the regeneration tower (7), flows downward through the packing layer, and countercurrently contacts with the rising steam generated by the bottom reboiler (8), decomposing acidic gases such as H2S and CO2. The regenerated lean amine liquid is collected in the tower bottom, pressurized by the lean liquid circulation pump (11), and then divided into two.

8. A process for removing organic sulfur from coke oven gas according to claim 7, characterized in that: The method further comprises the steps of: S4: A portion of the acidic gases such as H2S and CO2 are returned to the top of the desulfurization tower (3) for recycling, and the other portion is heated by the reboiler (8) to form a steam rising gas source; the acidic gases separated are discharged from the top of the tower, cooled by the condenser, and then enter the gas-liquid separator. The separated acidic gases are sent to the sulfur recovery unit; S5: The sulfur resource recovery system is used to process the acid gas desorbed from the regeneration tower (7) and convert the sulfur therein into sulfur. In the composite complex iron tail gas treatment device, all the sulfur is converted into sulfur. The acid gas enters from the bottom of the oxidation reaction tower (13) and contacts with the complex iron solution from top to bottom in countercurrent; S6: H2S in the acid gas is oxidized to elemental sulfur and dissolved in the solution. After desulfurization, CO2 gas is discharged from the top of the tower, and the sulfur-rich complex iron solution flows out from the bottom of the tower and enters the sulfur separation unit (15) after passing through the solution circulation pump (14) to separate the elemental sulfur and oxidize and regenerate the complex iron.

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