Coke-oven gas purification treatment system

Abstract

The utility model relates to the technical field of ferrous metallurgy, in particular to a coke-oven gas purification treatment system which comprises a first TSA device and a second TSA device, the first TSA device is provided with a coke-oven gas inlet; the coke-oven gas compression device is connected with a coke-oven gas outlet of the first TSA device; the second TSA device is connected with a coke-oven gas outlet of the coke-oven gas compression device; the hydrogenation fine desulfurization device is connected with a coke-oven gas outlet of the second TSA device; and the hydrogenation fine desulfurization device is provided with a purified coke-oven gas outlet. The system provided by the utility model meets the impurity content requirement on the coke-oven gas when the gas-based shaft furnace is used for producing HBI products, and can avoid carbon deposition of the furnace tube of the heating furnace at high temperature, so that the service life and efficiency of the furnace tube of the heating furnace are prevented from being influenced, and the HBI product quality is also prevented from being reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of iron and steel metallurgy, in particular to a coke oven gas purification and treatment system. Background Technique

[0002] Solving the energy problem well is the fundamental path to achieve carbon emission reduction. Implementing the energy structure adjustment of "replacing carbon with hydrogen" in the iron and steel industry is an effective solution for low-carbon transformation. The molar content of H2 in coke oven gas is more than 50%, meeting the requirement of the H2 content in the raw material gas for low-carbon hydrogen metallurgy. However, the impurity content in coke oven gas is high, generally including sulfur, tar, naphthalene, benzene and unsaturated hydrocarbons. Specifically, the tar content can reach 20mg / Nm 3 , the dust can reach 10mg / Nm 3 , the benzene can reach 4000mg / Nm 3 , the naphthalene can reach 350mg / Nm 3 , the hydrogen sulfide can reach 150mg / Nm 3 , the organic sulfur can reach 350mg / Nm 3 . Therefore, it is necessary to remove its impurities to meet the requirements of the quality of the reducing gas for the shaft furnace.

[0003] For the production of hot briquetted iron (HBI), due to the high temperature requirement for the pellets, at least 680°C, the scheme of pre-purifying the coke oven gas initially and then reforming the coke oven gas at the cone bottom of the shaft furnace cannot be adopted. Otherwise, it is easy to cause carbon deposition on the furnace tubes of the heating furnace at high temperature, affecting the service life and efficiency of the furnace tubes of the heating furnace. Content of the Utility Model

[0004] In view of this, the technical problem to be solved by the utility model is to provide a coke oven gas purification and treatment system, which can meet the requirements of the impurity content of the coke oven gas when producing HBI products by the shaft furnace, can avoid carbon deposition on the furnace tubes of the heating furnace at high temperature, thereby avoiding affecting the service life and efficiency of the furnace tubes of the heating furnace, and also avoiding the decline of the quality of HBI products.

[0005] The utility model provides a coke oven gas purification and treatment system, including:

[0006] A first TSA device; the first TSA device is provided with a coke oven gas inlet;

[0007] A coke oven gas compression device connected to the coke oven gas outlet of the first TSA device;

[0008] A second TSA device connected to the coke oven gas outlet of the coke oven gas compression device;

[0009] A hydrogenation fine desulfurization device connected to the coke oven gas outlet of the second TSA device; the hydrogenation fine desulfurization device is provided with a purified coke oven gas outlet.

[0010] Preferably, the first TSA device includes:

[0011] A desulfurization tower group; the desulfurization tower group is provided with a coke oven gas inlet;

[0012] An oil and naphthalene removal tower group, the coke oven gas inlet of the oil and naphthalene removal tower group is connected to the coke oven gas outlet of the desulfurization tower group; the coke oven gas outlet of the oil and naphthalene removal tower group is connected to the coke oven gas inlet of the coke oven gas compression device; the coke oven gas outlet of the oil and naphthalene removal tower group is also the inlet of the oil and naphthalene removal regenerated gas; the coke oven gas inlet of the oil and naphthalene removal tower group is also the outlet of the oil and naphthalene removal regenerated gas;

[0013] An oil and naphthalene removal regenerated gas heater, an oil and naphthalene removal regenerated gas heater is provided at the inlet of the oil and naphthalene removal regenerated gas;

[0014] An oil and naphthalene removal regenerated gas cooler, the regenerated gas inlet of the oil and naphthalene removal regenerated gas cooler is connected to the outlet of the oil and naphthalene removal regenerated gas;

[0015] An oil and naphthalene removal regenerated gas separator connected to the outlet of the oil and naphthalene removal regenerated gas cooler.

[0016] Preferably, the gas outlet of the oil and naphthalene removal regenerated gas separator is connected to the regenerated gas inlet of the coke oven;

[0017] The inlet of the oil and naphthalene removal regenerated gas of the oil and naphthalene removal tower group is connected to the outlet of the regenerated gas of the second TSA device.

[0018] Preferably, the oil and naphthalene removal tower group includes at least four oil and naphthalene removal towers.

[0019] Preferably, the second TSA device includes:

[0020] A debenzolization tower group; the coke oven gas inlet of the debenzolization tower group is connected to the coke oven gas outlet of the coke oven gas compression device; the coke oven gas outlet of the debenzolization tower group is connected to the coke oven gas inlet of the hydrofining desulfurization device; the coke oven gas outlet of the debenzolization tower group is also the inlet of the debenzolization regenerated gas; the coke oven gas inlet of the debenzolization tower group is also the outlet of the debenzolization regenerated gas;

[0021] A debenzolization regenerated gas heater, a debenzolization regenerated gas heater is provided at the inlet of the debenzolization regenerated gas;

[0022] A debenzolization regenerated gas cooler, the regenerated gas inlet of the debenzolization regenerated gas cooler is connected to the outlet of the debenzolization regenerated gas;

[0023] A debenzolization regenerated gas separator connected to the outlet of the debenzolization regenerated gas cooler.

[0024] Preferably, the regenerated gas outlet of the benzol removal regenerated gas separator is connected to the deoiling and denaphthalizing regenerated gas inlet of the first TSA unit.

[0025] Preferably, the benzol removal column group includes at least four benzol removal columns.

[0026] Preferably, the hydrofining desulfurization unit includes:

[0027] A pre-processor;

[0028] A heat exchanger; the cold gas inlet of the heat exchanger is connected to the coke oven gas outlet of the pre-processor;

[0029] A start-up electric heater connected to the hot gas outlet of the heat exchanger;

[0030] A pre-hydrogenation reaction assembly connected to the coke oven gas outlet of the start-up electric heater;

[0031] A first-stage hydrogenation reactor connected to the gas outlet of the pre-hydrogenation reaction assembly;

[0032] A steam generator connected to the gas outlet of the first-stage hydrogenation reactor; a branch pipeline is provided at the inlet of the steam generator, and the outlet of the branch pipeline is provided at the outlet of the steam generator;

[0033] A medium-temperature desulfurization tower group connected to the gas outlet of the steam generator;

[0034] A second-stage hydrogenation reactor connected to the gas outlet of the medium-temperature desulfurization tower group;

[0035] A fine desulfurization tower group connected to the gas outlet of the second-stage hydrogenation reactor; the gas outlet of the fine desulfurization tower group is connected to the hot gas inlet of the heat exchanger;

[0036] A cooler connected to the cold gas outlet of the heat exchanger;

[0037] A gas-liquid separator connected to the outlet of the cooler; the gas outlet of the gas-liquid separator is the purified coke oven gas outlet.

[0038] Preferably, the medium-temperature desulfurization tower group is connected in series between the first-stage hydrogenation reactor and the steam generator:

[0039] The medium-temperature desulfurization tower group is connected to the gas outlet of the first-stage hydrogenation reactor, the steam generator is connected to the gas outlet of the medium-temperature desulfurization tower group, and the second-stage hydrogenation reactor is connected to the gas outlet of the steam generator; a branch pipeline is provided at the inlet of the steam generator, and the outlet of the branch pipeline is provided at the outlet of the steam generator.

[0040] Preferably, the coke oven gas compression unit is a wet screw compressor.

[0041] The utility model provides a coke oven gas purification treatment system for producing hot briquetted iron with coke oven gas, including: a first TSA device; the first TSA device is provided with a coke oven gas inlet; a coke oven gas compression device connected to the coke oven gas outlet of the first TSA device; a second TSA device connected to the coke oven gas outlet of the coke oven gas compression device; a hydrodesulfurization device connected to the coke oven gas outlet of the second TSA device; the hydrodesulfurization device is provided with a purified coke oven gas outlet. The system provided by this application can meet the requirements for the impurity content of coke oven gas when producing HBI products with a gas-based shaft furnace, can avoid carbon deposition on the furnace tubes of the heating furnace at high temperatures, thereby avoiding affecting the service life and efficiency of the furnace tubes of the heating furnace, and also avoiding a decline in the quality of HBI products. Description of the Drawings

[0042] Figure 1 It is a coke oven gas purification treatment system diagram provided by an embodiment of the utility model;

[0043] Figure 2 It is a system diagram of the first TSA device provided by an embodiment of this application;

[0044] Figure 3 It is a system diagram of the second TSA device provided by an embodiment of this application;

[0045] Figure 4 It is a system diagram of the hydrodesulfurization device provided by an embodiment of this application. Detailed Embodiments

[0046] Next, in combination with the embodiments of the utility model, the technical solutions of the utility model will be clearly and completely described. Obviously, the described embodiments are only a part of the embodiments of the utility model, rather than all the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the utility model.

[0047] The utility model provides a coke oven gas purification treatment system, including:

[0048] A first TSA device; the first TSA device is provided with a coke oven gas inlet;

[0049] A coke oven gas compression device connected to the coke oven gas outlet of the first TSA device;

[0050] A second TSA device connected to the coke oven gas outlet of the coke oven gas compression device;

[0051] A hydrodesulfurization device connected to the coke oven gas outlet of the second TSA device; the hydrodesulfurization device is provided with a purified coke oven gas outlet.

[0052] Figure 1 The system diagram of the coke oven gas purification and treatment system provided for an embodiment of the present utility model.

[0053] The coke oven gas purification and treatment system provided by this application includes a first TSA device; the first TSA device is provided with a coke oven gas inlet. The coke oven gas inlet of the first TSA device is connected to the coke oven gas outlet of the coking plant. The first TSA device is used to remove tar, naphthalene, and perform rough benzene removal. The first TSA device includes a desulfurization tower group and an oil and naphthalene removal tower group connected in sequence. In the oil and naphthalene removal tower group, the number of oil and naphthalene removal towers ≥ 4. The regeneration gas outlet of the first TSA device is connected to the regeneration gas inlet of the coke oven.

[0054] In some embodiments of this application, the first TSA device includes:

[0055] The desulfurization tower group; the desulfurization tower group is provided with a coke oven gas inlet;

[0056] The oil and naphthalene removal tower group, the coke oven gas inlet of the oil and naphthalene removal tower group is connected to the coke oven gas outlet of the desulfurization tower group; the coke oven gas outlet of the oil and naphthalene removal tower group is connected to the coke oven gas inlet of the coke oven gas compression device; the coke oven gas outlet of the oil and naphthalene removal tower group is also the inlet of the oil and naphthalene removal regeneration gas; the coke oven gas inlet of the oil and naphthalene removal tower group is also the outlet of the oil and naphthalene removal regeneration gas;

[0057] The oil and naphthalene removal regeneration gas heater, the oil and naphthalene removal regeneration gas heater is provided at the inlet of the oil and naphthalene removal regeneration gas;

[0058] The oil and naphthalene removal regeneration gas cooler, the regeneration gas inlet of the oil and naphthalene removal regeneration gas cooler is connected to the regeneration gas outlet of the oil and naphthalene removal regeneration gas;

[0059] The oil and naphthalene removal regeneration gas separator connected to the regeneration gas outlet of the oil and naphthalene removal regeneration gas cooler.

[0060] Figure 2 The system diagram of the first TSA device provided for an embodiment of this application. Among them, 11 is the desulfurization tower group; 12 (including 12-A, 12-B, 12-C, 12-D) is the oil and naphthalene removal tower group, where 12-A is the No. 1 oil and naphthalene removal tower, 12-B is the No. 2 oil and naphthalene removal tower, 12-C is the No. 3 oil and naphthalene removal tower, and 12-D is the No. 4 oil and naphthalene removal tower; 13 is the oil and naphthalene removal regeneration gas heater; 14 is the oil and naphthalene removal regeneration gas cooler; 15 is the oil and naphthalene removal regeneration gas separator.

[0061] In some embodiments of the present application, the desulfurization tower group 11 includes more than two desulfurization towers. The number of desulfurization towers provided is related to the H2S content in the coke oven gas from the coking plant and the replacement cycle of the desulfurizing agent. Generally speaking, the higher the H2S content in the coke oven gas from the coking plant, the longer the replacement cycle of the desulfurizing agent, and the more desulfurization towers are required.

[0062] The coke oven gas is the coke oven gas from the coking plant. After the desulfurization treatment by the desulfurization tower group 11, the H2S content in the coke oven gas is not higher than 20 mg / Nm 3 . In some embodiments of the present application, the coke oven gas enters the desulfurization tower group 11 at a pressure of 3 - 7 kPaG.

[0063] In some embodiments of the present application, the oil and naphthalene removal tower group 12 includes at least four oil and naphthalene removal towers, and the oil and naphthalene removal towers are adsorption towers well-known to those skilled in the art that can be used for oil and naphthalene removal. The oil and naphthalene removal tower group 12 is set up by combining at least four oil and naphthalene removal towers. The operation process of each adsorption tower includes an adsorption process and a regeneration process.

[0064] In some embodiments of the present application, the oil and naphthalene removal regeneration gas inlet of the oil and naphthalene removal tower group 12 is connected to the regeneration gas outlet of the second TSA device. In some embodiments, the oil and naphthalene removal regeneration gas inlet of the oil and naphthalene removal tower group 12 is simultaneously connected to the regeneration gas outlet of the second TSA device and other regeneration gas outlets.

[0065] After the adsorbent in the oil and naphthalene removal tower has been adsorbed for a period of time, it will lose its adsorption capacity. At this time, it needs to be regenerated to restore the adsorption capacity of the adsorbent. Therefore, the operation process of the oil and naphthalene removal tower can be divided into an adsorption process and a regeneration process.

[0066] In the adsorption process (A1) stage, the coke oven gas treated by the desulfurization tower group 11 enters the oil and naphthalene removal tower group 12 for adsorption. When the mass transfer zone front (also known as the adsorption front) of the adsorbed impurities reaches the reserved section at the outlet of the adsorbent bed layer, the adsorption stops and the regeneration process is entered.

[0067] The regeneration gas used in the regeneration process can be a part of the coke oven gas purified by the second TSA device. Exemplarily, the regeneration gas can account for 14% - 16% (volume ratio) of the total purified gas volume. Of course, in actual applications, regeneration gas can also be introduced additionally.

[0068] The regeneration process may include:

[0069] 1 - 1) Pressure relief process (D1)

[0070] After the adsorption ends, the process of discharging the pressure in the adsorption tower (oil and naphthalene removal tower) against the adsorption direction to match the force of the regeneration gas.

[0071] 1-2) Heating process (H1)

[0072] After the pressure relief is completed, the regenerated gas from the adsorption tower (oil and naphthalene removal tower) in the cooling process is heated by the oil and naphthalene removal regenerated gas heater 13, and then blows the adsorbent bed layer against the adsorption direction, so that the adsorbed impurities can be desorbed at a high temperature state. The desorbed impurities flow out from the bottom of the adsorption tower to the oil and naphthalene removal regenerated gas cooler 14 along with the regenerated gas, and can be sent to the coke oven after cooling and separation by the oil and naphthalene removal regenerated gas separator 15.

[0073] In specific implementation, the regenerated gas can be heated to about 200 °C by the oil and naphthalene removal regenerated gas heater 13.

[0074] In specific implementation, when the bottom outlet gas temperature of the adsorption tower (oil and naphthalene removal tower) is higher than the first set temperature (for example, 170 °C), the heating process can be ended.

[0075] 1-3) Cooling process (C1)

[0076] After the heating is completed, the regenerated gas at normal temperature is used to blow the adsorbent bed layer of the oil and naphthalene removal tower against the adsorption direction, so that the adsorbent is cooled down to restore the adsorption capacity.

[0077] The regenerated gas after cooling treatment can be used as the regenerated gas of another adsorption tower (oil and naphthalene removal tower) in the heating process, or can be directly sent to the coke oven after passing through the oil and naphthalene removal regenerated gas cooler 14 and the oil and naphthalene removal regenerated gas separator 15.

[0078] In specific implementation, when the bottom outlet gas temperature of the adsorption tower (oil and naphthalene removal tower) is lower than the second set temperature (for example, 40 °C), the cooling process can be ended.

[0079] 1-4) Displacement process (R1)

[0080] After the cooling is completed, the regenerated gas in the adsorption tower (oil and naphthalene removal tower) is displaced by the regenerated gas against the adsorption direction. Through displacement, the stability of the gas outlet of the adsorption tower after entering the adsorption process can be ensured.

[0081] In specific implementation, among the aforementioned at least four adsorption towers (oil and naphthalene removal towers), at least two adsorption towers (oil and naphthalene removal towers) are in the adsorption process, and at least two adsorption towers (oil and naphthalene removal towers) are in the regeneration process. In this way, it can be ensured that the oil and naphthalene removal tower group 12 realizes continuous treatment of coke oven gas for removing tar, dust, naphthalene, and benzene.

[0082] Each adsorption tower of the oil and naphthalene removal tower group 12 can control the operation of the adsorption tower by controlling the opening and closing states of the valves of each passage through a time program. Figure 2In the illustrated example, the deoiling and denaphthalene removal tower group 12 is provided with four adsorption towers, namely, the No. 1 deoiling and denaphthalene removal tower 12-A, the No. 2 deoiling and denaphthalene removal tower 12-B, the No. 3 deoiling and denaphthalene removal tower 12-C, and the No. 4 deoiling and denaphthalene removal tower 12-D. As can be seen from Figure 2 it, each adsorption tower is provided with a gas flow path corresponding to each of the above processes, and relevant valves are provided on each flow path. The operation process of the adsorption tower can be adjusted by controlling the opening and closing of the relevant valves on these flow paths.

[0083] Taking Figure 2 the illustration as an example, a timing operation of four adsorption towers (deoiling and denaphthalene removal towers) is described.

[0084] Table 1 Timing operation table of four adsorption towers in the deoiling and denaphthalene removal tower group 12

[0085]

[0086] Referring to Table 1 above, "A1" in Table 1 represents the adsorption process, "D1" represents the pressure relief process, "H1" represents the heating process, "C1" represents the cooling process, and "R1" represents the displacement process.

[0087] As can be seen from Table 1, the No. 1 deoiling and denaphthalene removal tower 12-A is in the adsorption process at the 1st to 6th timings, in the pressure relief process at the 7th timing, in the heating process at the 8th timing, in the cooling process at the 9th to 11th timings, and in the displacement process at the 12th timing; the No. 2 deoiling and denaphthalene removal tower 12-B is in the cooling process at the 12th timing, the 1st to 2nd timings, in the displacement process at the 3rd timing, in the adsorption process at the 4th to 9th timings, in the pressure relief process at the 10th timing, and in the heating process at the 11th timing; the No. 3 deoiling and denaphthalene removal tower 12-C is in the pressure relief process at the 1st timing, in the heating process at the 2nd timing, in the cooling process at the 3rd to 5th timings, in the displacement process at the 6th timing, and in the adsorption process at the 7th to 12th timings; the No. 4 deoiling and denaphthalene removal tower 12-D is in the adsorption process at the 10th to 12th, 1st to 3rd timings, in the pressure relief process at the 4th timing, in the heating process at the 5th timing, in the cooling process at the 6th to 8th timings, and in the displacement process at the 9th timing.

[0088] By comparison, it can be seen that at each timing, two adsorption towers are in the adsorption process and two adsorption towers are in the regeneration process. In this way, it can be ensured that the deoiling and denaphthalene removal tower group 12 can perform continuous adsorption operation on the coke oven gas to achieve continuous removal of tar, naphthalene, dust, and benzene impurities.

[0089] In specific implementation, the adsorbents used in the adsorption towers of the deoiling and denaphthalene removal tower group 12 are the same, and activated carbon adsorbent can be selected as the adsorbent.

[0090] During specific implementation, the setting of the oil and naphthalene removal tower group 12 enables the naphthalene content in the coke oven gas after being treated by the oil and naphthalene removal tower group 12 to be no higher than 2 mg / Nm 3 , the tar content to be no higher than 2 mg / Nm 3 , the dust content to be no higher than 1 mg / Nm 3 , and the benzene content to be no higher than 2000 mg / Nm 3 .

[0091] The system for producing hot briquetted iron from coke oven gas provided by this application further includes a coke oven gas compression device connected to the coke oven gas outlet of the first TSA device.

[0092] The coke oven gas by-produced from the coking plant is generally at normal temperature and slightly positive pressure. Since the operating pressure of the gas-based shaft furnace is 8 - 10 barA, therefore, the coke oven gas needs to be compressed to meet the required pressure of the shaft furnace. The coke oven gas compression device is used to compress the coke oven gas to meet the required pressure of the shaft furnace.

[0093] In some embodiments of this application, the coke oven gas compression device is a wet screw compressor with water injection, which can be commercially available. The coke oven gas outlet pressure of the coke oven gas compression device ≥ 1.1 MPaG.

[0094] The system for producing hot briquetted iron from coke oven gas provided by this application further includes a second TSA device connected to the coke oven gas outlet of the coke oven gas compression device. The second TSA device is used for fine benzene removal. The second TSA device includes a debenzolization tower. The number of trays of the debenzolization tower ≥ 4. The debenzolization tower is filled with an adsorbent, which is an activated carbon adsorbent, and its main function is benzene removal. The remaining benzene in the coke oven gas is adsorbed and removed under the action of the adsorbent of the second TSA device.

[0095] The oil and naphthalene removal regeneration gas heater 13 is a conventional non-standard shell-and-tube gas heater, the oil and naphthalene removal regeneration gas cooler 14 is a conventional non-standard shell-and-tube gas cooler, and the oil and naphthalene removal regeneration gas separator 15 is a conventional non-standard gas separator.

[0096] In some embodiments of this application, the second TSA device includes:

[0097] A debenzolization tower group; the coke oven gas inlet of the debenzolization tower group is connected to the coke oven gas outlet of the coke oven gas compression device; the coke oven gas outlet of the debenzolization tower group is connected to the coke oven gas inlet of the hydrodesulfurization unit; the coke oven gas outlet of the debenzolization tower group is also the debenzolization regeneration gas inlet; the coke oven gas inlet of the debenzolization tower group is also the debenzolization regeneration gas outlet;

[0098] A debenzolization regeneration gas heater, which is provided at the debenzolization regeneration gas inlet;

[0099] The benzol removal regenerated gas cooler, the regenerated gas inlet of the benzol removal regenerated gas cooler is connected to the regenerated gas outlet;

[0100] The benzol removal regenerated gas separator connected to the regenerated gas outlet of the benzol removal regenerated gas cooler.

[0101] Figure 3 It is the system diagram of the second TSA device provided by an embodiment of the present application. Among them, 22 (including 22-A, 22-B, 22-C, 22-D) is the benzol removal tower group, where 22-A is the No. 1 benzol removal tower, 22-B is the No. 2 benzol removal tower, 22-C is the No. 3 benzol removal tower, and 22-D is the No. 4 benzol removal tower; 23 is the benzol removal regenerated gas heater; 24 is the benzol removal regenerated gas cooler; 25 is the benzol removal regenerated gas separator.

[0102] In some embodiments of the present application, the benzol removal tower group 22 includes at least four benzol removal towers, and the benzol removal towers are adsorption towers well-known to those skilled in the art that can be used for benzol removal. The benzol removal tower group 22 is jointly arranged by at least four benzol removal towers. The operation process of each adsorption tower includes an adsorption process and a regeneration process.

[0103] After the adsorbent in the benzol removal tower has been adsorbed for a period of time, it no longer has the adsorption capacity. At this time, it needs to be regenerated to restore the adsorption capacity of the adsorbent. Therefore, the operation process of the benzol removal tower can be divided into an adsorption process and a regeneration process.

[0104] In the adsorption process (A2) stage, the coke oven gas treated by the coke oven gas compression device enters the benzol removal tower group 22 for adsorption. When the mass transfer zone front (also known as the adsorption front) of the adsorbed impurities reaches the reserved section at the outlet of the adsorbent bed layer, the adsorption stops and the regeneration process is transferred to.

[0105] The regenerated gas used in the regeneration process can be a part of the coke oven gas purified by the second TSA device. Exemplarily, the regenerated gas can account for 14% - 16% (volume ratio) of the total purified gas volume. Of course, in actual applications, regenerated gas can also be introduced additionally.

[0106] The regeneration process may include:

[0107] 2-1) Pressure relief process (D2)

[0108] After the adsorption ends, the process of discharging the pressure in the adsorption tower (benzol removal tower) against the adsorption direction to match the pressure of the regenerated gas.

[0109] 2-2) Heating process (H2)

[0110] After the pressure relief is completed, the regenerated gas from the adsorption tower (benzene stripper) in the cooling process is heated by the benzene stripper regenerated gas heater 23 and then purges the adsorbent bed against the adsorption direction, so that the adsorbed impurities can be desorbed at a high temperature state. The desorbed impurities flow out from the bottom of the adsorption tower along with the regenerated gas to the benzene stripper regenerated gas cooler 24, and can be sent to the coke oven after cooling and separation by the benzene stripper regenerated gas separator 25.

[0111] In specific implementation, the regenerated gas can be heated to about 200 °C by the benzene stripper regenerated gas heater 23.

[0112] In specific implementation, when the bottom outlet gas temperature of the adsorption tower (benzene stripper) is higher than the first set temperature (for example, 170 °C), the heating process can be ended.

[0113] 2-3) Cooling process (C2)

[0114] After the heating is completed, the regenerated gas at normal temperature is used to purge the adsorbent bed of the benzene stripper against the adsorption direction, so that the adsorbent is cooled down to restore the adsorption capacity.

[0115] The regenerated gas after cooling treatment can be used as the regenerated gas of another adsorption tower in the heating process, or can be directly sent to the first TSA device after passing through the cooler 24 and the regenerated gas gas-liquid separator 25.

[0116] In specific implementation, when the bottom outlet gas temperature of the adsorption tower is lower than the second set temperature (for example, 40 °C), the cooling process can be ended.

[0117] 2-4) Replacement process (R2)

[0118] After the cooling is completed, the regenerated gas in the adsorption tower (benzene stripper) is replaced with the regenerated gas against the adsorption direction. Through replacement, the stability of the gas outlet of the adsorption tower can be ensured after entering the adsorption process.

[0119] In specific implementation, among the at least four adsorption towers (benzene strippers), at least two adsorption towers (benzene strippers) are in the adsorption process, and at least two adsorption towers (benzene strippers) are in the regeneration process. In this way, it can be ensured that the benzene stripper group 22 can continuously remove benzene from the coke oven gas.

[0120] Each adsorption tower of the benzene stripper group 22 can control the operation of the adsorption tower by controlling the opening and closing states of the valves of each passage through a time program. Figure 3 In the shown example, the benzene stripper group 22 of the second TSA device is provided with four adsorption towers, namely the No. 1 benzene stripper 22-A, the No. 2 benzene stripper 22-B, the No. 3 benzene stripper 22-C and the No. 4 benzene stripper 22-D. From Figure 3It can be seen that each adsorption tower is provided with a gas flow path corresponding to each of the above processes, and relevant valves are arranged on each flow path. The operating process of the adsorption tower can be adjusted by controlling the opening and closing of the relevant valves on these flow paths.

[0121] Taking the following Figure 3 as an example, a timing operation of four adsorption towers (dephenolization towers) will be described.

[0122] Table 2 - Timing operation table of four adsorption towers in the adsorption tower group

[0123] Timing sequence 1 2 3 4 5 6 7 8 9 10 11 12 No. 1 Dephenolization Tower A2 A2 A2 A2 A2 A2 D2 H2 C2 C2 C2 R2 No. 2 Dephenolization Tower C2 C2 R2 A2 A2 A2 A2 A2 A2 D2 H2 C2 No. 3 Dephenolization Tower D2 H2 C2 C2 C2 R2 A2 A2 A2 A2 A2 A2 No. 4 Dephenolization Tower A2 A2 A2 D2 H2 C2 C2 C2 R2 A2 A2 A2

[0124] Referring to Table 2 above, "A2" in Table 2 represents the adsorption process, "D2" represents the pressure relief process, "H2" represents the heating process, "C2" represents the cooling process, and "R2" represents the replacement process.

[0125] It can be seen from Table 2 that the No. 1 dephenolization tower 22 - A is in the adsorption process at the 1st to 6th timings, in the pressure relief process at the 7th timing, in the heating process at the 8th timing, in the cooling process at the 9th to 11th timings, and in the replacement process at the 12th timing; the No. 2 dephenolization tower 22 - B is in the cooling process at the 12th timing, the 1st to 2nd timings, in the replacement process at the 3rd timing, in the adsorption process at the 4th to 9th timings, in the pressure relief process at the 10th timing, and in the heating process at the 11th timing; the No. 3 dephenolization tower 22 - C is in the pressure relief process at the 1st timing, in the heating process at the 2nd timing, in the cooling process at the 3rd to 5th timings, in the replacement process at the 6th timing, and in the adsorption process at the 7th to 12th timings; the No. 4 dephenolization tower 22 - D is in the adsorption process at the 10th to 12th, 1st to 3rd timings, in the pressure relief process at the 4th timing, in the heating process at the 5th timing, in the cooling process at the 6th to 8th timings, and in the replacement process at the 9th timing.

[0126] By comparison, it can be seen that at each timing, two adsorption towers are in the adsorption process and two adsorption towers are in the regeneration process. In this way, it can be ensured that the dephenolization tower group 22 can perform continuous adsorption operations on the coke oven gas to achieve continuous dephenolization treatment.

[0127] In specific implementation, the adsorbents used in the adsorption towers of the dephenolization tower group 22 are the same, and activated carbon adsorbents can be selected as the adsorbents.

[0128] In specific implementation, the setting of the dephenolization tower group 22 ensures that the benzene content in the coke oven gas after being treated by the dephenolization tower group 22 is not higher than 10 mg / Nm 3 .

[0129] The debenzolized regenerated gas heater 23 is a conventional non-standard shell-and-tube gas heater, the debenzolized regenerated gas cooler 24 is a conventional non-standard shell-and-tube gas cooler, and the debenzolized regenerated gas separator 25 is a conventional non-standard gas separator. The system for producing hot briquetted iron using coke oven gas provided in this application further includes a hydrodesulfurization unit connected to the coke oven gas outlet of the second TSA unit; the hydrodesulfurization unit is provided with a purified coke oven gas outlet.

[0130] In some embodiments of this application, the hydrodesulfurization unit includes:

[0131] A pre-processor;

[0132] A heat exchanger; the cold gas inlet of the heat exchanger is connected to the coke oven gas outlet of the pre-processor;

[0133] A start-up electric heater connected to the hot gas outlet of the heat exchanger;

[0134] A pre-hydrogenation reaction assembly connected to the coke oven gas outlet of the start-up electric heater;

[0135] A primary hydrogenation reactor connected to the gas outlet of the pre-hydrogenation reaction assembly;

[0136] A steam generator connected to the gas outlet of the primary hydrogenation reactor; a branch pipeline is provided at the inlet of the steam generator, and the outlet of the branch pipeline is provided at the outlet of the steam generator;

[0137] A medium-temperature desulfurization tower group connected to the gas outlet of the steam generator;

[0138] A secondary hydrogenation reactor connected to the gas outlet of the medium-temperature desulfurization tower group;

[0139] A fine desulfurization tower group connected to the gas outlet of the secondary hydrogenation reactor; the gas outlet of the fine desulfurization tower group is connected to the hot gas inlet of the heat exchanger;

[0140] A cooler connected to the cold gas outlet of the heat exchanger;

[0141] A gas-liquid separator connected to the outlet of the cooler; the gas outlet of the gas-liquid separator is the purified coke oven gas outlet.

[0142] Figure 4System diagram of the hydrodesulfurization device provided for an embodiment of the present application. Among them, 31 is a pre-processor; 32 (including 32-A and 32-B) is a pre-hydrogenation reaction assembly, where 32-A is the first pre-hydrogenation reactor and 32-B is the second pre-hydrogenation reactor; 33 is a primary hydrogenation reactor; 34 (including 34-A and 34-B) is a medium-temperature desulfurization tower group, where 34-A is the first medium-temperature desulfurization tower and 34-B is the second medium-temperature desulfurization tower; 35 is a secondary hydrogenation reactor; 36 (including 36-A and 36-B) is a fine desulfurization tower group, where 36-A is the first fine desulfurization tower and 36-B is the second fine desulfurization tower; 37 is a heat exchanger; 38 is a start-up electric heater; 39 is a steam generator; 40 is a cooler; 41 is a gas-liquid separator.

[0143] In the present application, the coke oven gas treated by the second TSA device enters the pre-processor 31. After the pre-processor 31 removes impurities such as oil and dust in the coke oven gas, it then enters the start-up electric heater 38 after being heated to 240 - 260 °C by the heat exchanger 37. The heat source of the heat exchanger 37 comes from the heat of the reaction product. Generally, the start-up electric heater 38 does not heat, and the coke oven gas only passes through the start-up electric heater 38; when the operating load of the device is low and the heat of the reaction product in the start-up electric heater 38 is not sufficient to heat the raw material gas to the target temperature, the resistance wire of the start-up electric heater 38 starts to work to ensure that the coke oven gas enters the pre-hydrogenation reaction assembly 32 at a temperature of 240 - 260 °C.

[0144] The gas coming out of the pre-hydrogenation reaction assembly 32 enters the primary hydrogenation reactor 33. The coke oven gas coming out of the primary hydrogenation reactor can reach 380 - 405 °C, and at this time, most of the organic sulfur is converted into hydrogen sulfide. Before entering the medium-temperature desulfurization tower group 34, the heat needs to be removed. Therefore, after the primary hydrogenation, the coke oven gas is divided into two paths. One part is cooled by the steam generator 39 and then mixed with the remaining part of the gas. The flow rate of the gas entering the steam generator 39 is adjusted to ensure that the mixed gas enters the medium-temperature desulfurization tower group 34 at about 280 °C. The medium-temperature desulfurization tower group 34 is provided with a zinc oxide bed layer. The present application has no special requirements for the thickness of the zinc oxide bed layer, and the specifications of the desulfurization tower are determined according to the content of H2S and the gas flow rate. In the medium-temperature desulfurization tower group 34, the sulfur in hydrogen sulfide is adsorbed by the zinc oxide bed layer.

[0145] The coke oven gas exiting the medium-temperature desulfurization tower group 34 enters the secondary hydrogenation reactor 35, where the remaining organic sulfur is converted again. Since the content of the remaining organic sulfur is not much, the temperature rise during secondary hydrogenation is relatively low, and the outlet gas temperature is 340 - 360 °C. Therefore, there is no need to extract heat, and it directly enters the fine desulfurization tower group 36 to remove the generated H2S, ensuring that the H2S content in the gas is < 0.1 ppm. After the heat of the outlet purified gas is recovered by the heat exchanger 37, it enters the cooler 40 and is cooled to about 40 °C, and then enters the gas-liquid separator 41 for gas-liquid separation. The separated gas is used as the raw material gas for the shaft furnace reaction and is supplemented into the process gas system for the production of HBI. The following reactions occur in the pre-hydrogenation reaction module 32, the primary hydrogenation reactor 33, and the secondary hydrogenation reactor 35, and the reaction formulas are as follows:

[0146] COS + H2 → CO + H2S;

[0147] CS2 + 4H2 → CH4 + 2H2S;

[0148] C4H4S + 4H2 → C4H 10 + H2S.

[0149] After the hydrogenation reaction, the organic sulfur in the coke oven gas is converted into inorganic sulfur H2S. At this time, desulfurization equipment can be used to remove the inorganic sulfur H2S so that the total sulfur content in the treated coke oven gas meets the requirements for the production of HBI in the gas-based shaft furnace.

[0150] Under the action of the hydrogenation catalyst (such as iron molybdenum + nickel cobalt molybdenum catalyst), the following reactions will also occur in the coke oven gas:

[0151] 2H2 + O2 → 2H2O; CO + 3H2 → CH4 + H2O.

[0152] That is: during the hydrogenation process, there is a methanation side reaction, and this reaction is an exothermic reaction. To prevent the system from running away with temperature, a steam generator 39 is set up to generate steam with boiler feed water to remove the reaction heat of the system.

[0153] In the initial operation stage after the start-up of the hydrogenation fine desulfurization device, the coke oven gas entering the pre-hydrogenation reaction module 32 can be heated first through the start-up electric heater 38 to reach the activation temperature of the hydrogenation reaction, which is beneficial to the progress of the hydrogenation reaction; after the device has been started for a period of time, due to the increase in the heat released by the hydrogenation reaction, through the setting of the start-up electric heater 38, the coke oven gas treated by the pre-hydrogenation reaction module 32 can be used to heat up the coke oven gas that has not yet entered the pre-hydrogenation reaction module 32 for heat exchange to ensure the temperature of the hydrogenation reaction. At this time, the start-up electric heater 38 can be turned off.

[0154] Through the setting of the heat exchanger 37, the heat generated by the hydrogenation reaction can be reasonably utilized and recovered, which can eliminate the long-term operation of the start-up electric heater 38 and is beneficial to energy conservation.

[0155] In practical applications, the start-up electric heater 38 can be an electric heater.

[0156] Figure 4 In the example, the pre-hydrogenation reaction assembly 32 includes two pre-hydrogenation reactors arranged in parallel, namely the first pre-hydrogenation reactor 32-A and the second pre-hydrogenation reactor 32-B; the coke oven gas is divided into two paths and enters the two pre-hydrogenation reactors respectively for pre-hydrogenation treatment, and then enters the first-stage hydrogenation reactor 33 together for first-stage hydrogenation treatment.

[0157] Specifically, during implementation, the total sulfur content of the coke oven gas treated by the hydrodesulfurization unit is not higher than 0.1 ppm (mol).

[0158] In addition to Figure 4 the example shown, in other embodiments, the desulfurization equipment (medium-temperature desulfurization tower and fine desulfurization tower) in the hydrodesulfurization unit can also adopt dry desulfurization equipment, or adopt a combination of dry desulfurization equipment and wet desulfurization equipment.

[0159] In some embodiments of the present application, the medium-temperature desulfurization tower group 34 is connected in series between the first-stage hydrogenation reactor 33 and the steam generator 39, that is, the medium-temperature desulfurization tower group 34 is arranged upstream of the steam generator 39. Specifically, it is:

[0160] The medium-temperature desulfurization tower group 34 is connected to the gas outlet of the first-stage hydrogenation reactor 33, the steam generator 39 is connected to the gas outlet of the medium-temperature desulfurization tower group 34, and the second-stage hydrogenation reactor 35 is connected to the gas outlet of the steam generator 39; a branch pipeline is provided at the inlet of the steam generator 39, and the outlet of the branch pipeline is provided at the outlet of the steam generator 39.

[0161] Exemplarily, in the medium-temperature desulfurization tower group 34, the number of medium-temperature desulfurization towers can be set to more than two, which is specifically related to the desulfurization demand.

[0162] Generally speaking, the sulfur capacity of the medium-temperature desulfurizer is high and the replacement period is long, while the sulfur capacity of the normal-temperature desulfurizer is relatively low and the replacement period is short. During implementation, it can be selected according to actual application requirements.

[0163] Exemplarily, in the fine desulfurization tower group 36, according to the organic sulfur concentration in the raw material gas, the number of fine desulfurization towers can be set to more than two.

[0164] In certain embodiments of the present application, a branch is provided on the pipeline between the second TSA device and the hydrodesulfurization unit, and the outlet of the branch is connected to the reflux gas inlet of the second TSA device. A part of the coke oven gas after benzene rectification is transported to the hydrodesulfurization unit, and the other part is recycled to the second TSA device for regeneration. When the temperature of the regeneration gas entering the adsorption tower during the regeneration process remains unchanged as it passes through this tower, it represents the end of the regeneration process.

[0165] In certain embodiments of the present application, the regeneration gas outlet of the second TSA device is connected to the regeneration gas inlet of the first TSA device. The coke oven gas regenerated by the second TSA device is regenerated in the first TSA device. When the temperature of the regeneration gas entering the adsorption tower during the regeneration process remains unchanged as it passes through this tower, it represents the end of the regeneration process.

[0166] In certain embodiments of the present application, the regeneration gas outlet of the first TSA device is connected to the regeneration gas inlet of the coke oven. The coke oven gas regenerated by the first TSA device is recycled to the coke oven.

[0167] The pre-processor is a general conventional non-standard vertical pressure vessel equipment with packing; the pre-hydrogenation reactor, the first-stage hydrogenation reactor, and the second-stage hydrogenation reactor are all conventional non-standard hydrogenation reactors; the medium-temperature desulfurization tower is a conventional non-standard medium-temperature desulfurization tower; the fine desulfurization tower is a conventional non-standard desulfurization tower; the heat exchanger is a conventional non-standard shell-and-tube gas heat exchanger; the start-up electric heater is generally commercially available, the gas-liquid separator is a conventional non-standard equipment; the cooler is a conventional non-standard shell-and-tube gas cooler, and the steam generator is a conventional non-standard shell-and-tube heat exchanger.

[0168] The present utility model places no special restrictions on the raw material sources used above, and they can be generally commercially available.

[0169] To further illustrate the present utility model, the following provides a detailed description of a system for producing hot briquetted iron using coke oven gas according to the present utility model in conjunction with embodiments, but it should not be construed as limiting the protection scope of the present utility model.

[0170] Example 1

[0171] Using the coke oven gas purification treatment system for producing hot briquetted iron as shown in Figure 1 :

[0172] The components of the coke oven gas are shown in Table 3.

[0173] Table 3 Components of Coke Oven Gas and Coke Oven Gas at Some Treatment Stages

[0174]

[0175] In Table 3, the coke oven gas (2) after pre-purification (oil and naphthalene removal) is the coke oven gas processed by the first TSA unit; the coke oven gas (4) after pre-purification (benzene removal) is the coke oven gas processed by the second TSA unit; the coke oven gas (5) after fine desulfurization is the coke oven gas (or purified coke oven gas) processed by the hydrogenation fine desulfurization unit.

[0176] The coke oven gas (1) with a pressure of 3 - 7 kPaG from the coking plant and the components shown in Table 1 first enters Figure 2 the desulfurization tower of the first TSA unit shown. After being processed by the desulfurization tower, the content of H2S in the coke oven gas is 20 mg / Nm 3 ; then it enters the oil and naphthalene removal tower group (in the oil and naphthalene removal tower group, the number of oil and naphthalene removal towers = 4; the oil and naphthalene removal towers are filled with the first adsorbent, which is an activated carbon adsorbent) for oil removal, dust removal, naphthalene removal, and partial benzene removal. The oil and naphthalene removal towers are multi-towers that perform adsorption and regeneration operations in sequence to complete the removal of impurity tar, dust, naphthalene, and partial benzene, as well as the regeneration of the first adsorbent. For the components and impurity content of the coke oven gas after pre-purification (oil and naphthalene removal), see the coke oven gas (2) after pre-purification (oil and naphthalene removal) in Table 3.

[0177] The coke oven gas after oil and naphthalene removal enters the coke oven gas compression unit (a wet screw compressor with water injection) to pressurize the coke oven gas to meet the pressure requirements of the shaft furnace for the raw coke oven gas. The outlet pressure of the coke oven gas of the coke oven gas compression unit ≥ 1.1 MPaG.

[0178] The pressurized coke oven gas enters Figure 3 the benzene removal tower of the second TSA unit shown (the number of benzene removal towers = 4; the benzene removal towers are filled with the second adsorbent, which is an activated carbon adsorbent) for fine benzene removal; multiple benzene removal towers perform sequential control operations of adsorption, pressure relief, regeneration, and pressurization to complete the benzene removal of the coke oven gas cyclically. After benzene removal, the content of benzene in the coke oven gas ≤ 10 mg / Nm 3 . For the components and impurity content of the coke oven gas, see the coke oven gas (4) after pre-purification (benzene removal) in Table 1.

[0179] The regeneration gas required for the regeneration of the first TSA unit and the second TSA unit comes from a part of the coke oven gas after fine benzene removal (the part of the coke oven gas after fine benzene removal accounts for 15% of the total volume of the coke oven gas after all fine benzene removals). The part of the coke oven gas after fine benzene removal as the regeneration gas is first heated to about 200 °C and then enters the benzene removal tower for regeneration, then cooled to 40 °C, and after gas-liquid separation, the gas enters the oil and naphthalene removal tower group of the first TSA unit for the regeneration and removal of tar and naphthalene. The first TSA unit and the second TSA unit use the same part of the gas for step-by-step regeneration, which can save the amount of regeneration gas.

[0180] Another part of the coke oven gas after fine benzol removal enters Figure 4 the hydrodesulfurization unit shown in Figure 4 . The hydrodesulfurization unit is equipped with a hydrodesulfurization catalyst, which is an iron-molybdenum catalyst. The fine desulfurization section includes pre-hydrogenation, primary hydrogenation, a desulfurization tower, secondary hydrogenation, a fine desulfurization tower, and a heat exchange network. Through pre-hydrogenation, primary hydrogenation, and secondary hydrogenation, the organic sulfur in the coke oven gas is converted into inorganic sulfur. The reaction equations are as follows:

[0181] COS + H2 → CO + H2S;

[0182] CS2 + 4H2 → CH4 + 2H2S;

[0183] C4H4S + 4H2 → C4H 10 + H2S.

[0184] Under the action of the hydrodesulfurization catalyst, the following reactions also occur simultaneously in the coke oven gas:

[0185] 2H2 + O2 → 2H2O;

[0186] CO + 3H2 → CH4 + H2O.

[0187] After the hydrogenation reaction, the organic sulfur is converted into inorganic sulfur H2S. At this time, dry desulfurization or wet desulfurization + dry desulfurization can be used to meet the requirement that the total sulfur content in the coke oven gas < 0.1 ppmV.

[0188] The components and impurity contents of the coke oven gas treated by the hydrodesulfurization unit are shown in the coke oven gas after fine desulfurization (5) in Table 1. At this time, the requirement for the impurity content of the coke oven gas to produce HBI with a shaft furnace is met. This coke oven gas enters the inlet section of the process gas compressor of the shaft furnace to produce HBI products.

[0189] The above description of the disclosed embodiments enables those skilled in the art to implement or use the present invention. Various modifications to these embodiments will be obvious to those skilled in the art. The general principles defined herein can be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention will not be limited to these embodiments shown herein, but rather will be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A coke oven gas purification and treatment system, comprising: A first TSA device; The first TSA device is provided with a coke oven gas inlet; A coke oven gas compression device connected to the coke oven gas outlet of the first TSA device; A second TSA device connected to the coke oven gas outlet of the coke oven gas compression device; A hydrogenation fine desulfurization device connected to the coke oven gas outlet of the second TSA device; the hydrogenation fine desulfurization device is provided with a purified coke oven gas outlet.

2. The coke oven gas purification and treatment system according to claim 1, wherein, The first TSA device includes: A desulfurization tower group; the desulfurization tower group is provided with a coke oven gas inlet; An oil and naphthalene removal tower group, the coke oven gas inlet of the oil and naphthalene removal tower group is connected to the coke oven gas outlet of the desulfurization tower group; the coke oven gas outlet of the oil and naphthalene removal tower group is connected to the coke oven gas inlet of the coke oven gas compression device; the coke oven gas outlet of the oil and naphthalene removal tower group is also the inlet of the oil and naphthalene removal regenerated gas; the coke oven gas inlet of the oil and naphthalene removal tower group is also the outlet of the oil and naphthalene removal regenerated gas; An oil and naphthalene removal regenerated gas heater, which is provided at the inlet of the oil and naphthalene removal regenerated gas; An oil and naphthalene removal regenerated gas cooler, the regenerated gas inlet of the oil and naphthalene removal regenerated gas cooler is connected to the outlet of the oil and naphthalene removal regenerated gas; An oil and naphthalene removal regenerated gas separator connected to the regenerated gas outlet of the oil and naphthalene removal regenerated gas cooler.

3. The coke oven gas purification and treatment system according to claim 2, wherein The gas outlet of the oil and naphthalene removal regenerated gas separator is connected to the regenerated gas inlet of the coke oven; The inlet of the oil and naphthalene removal regenerated gas of the oil and naphthalene removal tower group is connected to the outlet of the regenerated gas of the second TSA device.

4. The coke oven gas purification treatment system according to claim 2, wherein, The oil and naphthalene removal tower group includes at least four oil and naphthalene removal towers.

5. The coke oven gas purification and treatment system according to claim 1, characterized in that, The second TSA device includes: A debenzolization tower group; the coke oven gas inlet of the debenzolization tower group is connected to the coke oven gas outlet of the coke oven gas compression device; the coke oven gas outlet of the debenzolization tower group is connected to the coke oven gas inlet of the hydrogenation fine desulfurization device; the coke oven gas outlet of the debenzolization tower group is also the inlet of the debenzolization regenerated gas; the coke oven gas inlet of the debenzolization tower group is also the outlet of the debenzolization regenerated gas; A debenzolization regenerated gas heater, which is provided at the inlet of the debenzolization regenerated gas; A debenzolization regenerated gas cooler, the regenerated gas inlet of the debenzolization regenerated gas cooler is connected to the outlet of the debenzolization regenerated gas; A debenzolization regenerated gas separator connected to the regenerated gas outlet of the debenzolization regenerated gas cooler.

6. The coke oven gas purification and treatment system according to claim 5, characterized in that, The regenerated gas outlet of the debenzolization regenerated gas separator is connected to the inlet of the oil and naphthalene removal regenerated gas of the first TSA device.

7. The coke oven gas purification treatment system according to claim 5, wherein The debenzolization tower group includes at least four debenzolization towers.

8. The coke oven gas purification treatment system according to claim 1, wherein, The hydrogenation fine desulfurization device includes: A pre-processor; A heat exchanger; the cold gas inlet of the heat exchanger is connected to the coke oven gas outlet of the pre-processor; A start-up electric heater connected to the hot gas outlet of the heat exchanger; A pre-hydrogenation reaction component connected to the coke oven gas outlet of the start-up electric heater; A first-stage hydrogenation reactor connected to the gas outlet of the pre-hydrogenation reaction component; A steam generator connected to the gas outlet of the first-stage hydrogenation reactor; a branch pipeline is provided at the inlet of the steam generator, and the outlet of the branch pipeline is provided at the outlet of the steam generator; A medium-temperature desulfurization tower group connected to the gas outlet of the steam generator; A secondary hydrogenation reactor connected to the gas outlet of the medium-temperature desulfurization tower group; A fine desulfurization tower group connected to the gas outlet of the secondary hydrogenation reactor; the gas outlet of the fine desulfurization tower group is connected to the hot gas inlet of the heat exchanger; A cooler connected to the cold gas outlet of the heat exchanger; A gas-liquid separator connected to the outlet of the cooler; the gas outlet of the gas-liquid separator is the purified coke oven gas outlet.

9. The coke oven gas purification and treatment system according to claim 8, characterized in that, The medium-temperature desulfurization tower group is connected in series between the primary hydrogenation reactor and the steam generator: The medium-temperature desulfurization tower group is connected to the gas outlet of the primary hydrogenation reactor, the steam generator is connected to the gas outlet of the medium-temperature desulfurization tower group, and the secondary hydrogenation reactor is connected to the gas outlet of the steam generator; a branch pipeline is provided at the inlet of the steam generator, and the outlet of the branch pipeline is provided at the outlet of the steam generator.

10. The coke oven gas purification treatment system according to claim 1, characterized in that, The coke oven gas compression device is a wet screw compressor.

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