CN109609219B - A kind of coking tail gas treatment method and device - Google Patents

Abstract

The invention discloses a coking tail gas treatment method and device, comprising the following steps and devices: sealing or nitrogen-filling a storage tank storing the coking tail gas; In the buffer tank, the initial dehydration, denaphthalene and detar are cooled in the buffer tank; the coking tail gas is sucked from the buffer tank to the Venturi mixer where the coking tail gas is removed, and the coking tail gas is fed into the Venturi mixer. Hydrogen source; discharge the gas mixed in the Venturi mixer into the deoxygenation tank for catalytic hydrodeoxidation; discharge the qualified coking tail gas into the gas main pipe of the gas purification system of the coking plant, or into the tail gas treatment system in the later stage . The method performs hydrodeoxidation on the collected coking tail gas with high oxygen content, thereby reducing the oxygen content in the coking tail gas, reducing the oxygen content of the coking tail gas to below 0.5%, so that the coking tail gas can directly enter the gas purification system of the coking plant for further Purification treatment.

Description

A kind of coking tail gas treatment method and device

technical field

The invention belongs to the technical field of coking equipment tail gas treatment, and relates to a coking tail gas treatment method and device.

Background technique

Coking generally refers to the process of carbonization and zooming of organic substances. In a coking plant, coking coal goes through the coking process, producing chemical products such as coke, coal tar, coke oven gas, and crude benzene. The gas purification process of coking production includes condensation blast section, ammonium sulfate section, desulfurization section, debenzene section, tank farm, etc. In addition, coking products include tar processing, crude benzene refining, crude phenol distillation, industrial naphthalene production, and asphalt. Therefore, the composition of coking tail gas is very complex. In addition to the vast majority of water vapor, it also includes various macromolecular polycyclic hydrocarbons or fused ring hydrocarbons and small molecular alkanes and olefins, as well as hydrogen sulfide, organic sulfur and ammonia. and many other toxic and harmful gases.

The traditional design of the intermediate tank, water sealing tank, raw material tank, product tank, tar ammonia water separation tank, and loading and unloading station exhaust gas of coking production are all unorganized emission, that is, a emission pipe is set on the top of the tank to directly discharge the coking tail gas into the air. , causing air pollution. The "Coking Chemical Industry Pollutant Emission Standard" (GB 16171-2012) requires that the exhaust gas from chemical chemical material tanks and tanks should be collected to the gas system recovery or purification facility. To implement the above requirements, equipment such as tanks must be sealed for exhaust gas collection. Some storage tanks containing Class A and _B materials even require nitrogen sealing facilities.

In the existing coking plant, only the gas purification system has hundreds of exhaust gas collection points. The properties of the storage materials in the tanks are different, the storage environments are different, the storage tank conditions (such as tank top corrosion and leakage) are different, and the volume of the storage tanks is different. The collection system and the composition of the exhaust gas are complex, and the exhaust gas collection process cannot ensure that the oxygen content in the exhaust gas is within a safe range, and the exhaust gas cannot be collected to the gas system for recovery; because the oxygen content in the gas is less than 0.6% according to the specification requirements, otherwise it will cause safety hazards, and at the same time It will cause frequent trips of the electric tar trap, affecting normal production, and collecting exhaust gas and sending it to subsequent treatment facilities will also cause certain hidden dangers for subsequent exhaust gas purification.

SUMMARY OF THE INVENTION

The technical problem solved by the present invention is to provide a coking tail gas treatment method and device, which can reduce the oxygen content of the coking tail gas, realize the airtight collection of the coking tail gas, and avoid the fugitive emission of the coking tail gas.

The present invention is realized through the following technical solutions: a coking tail gas treatment method, comprising the following steps:

(1) Sealing or filling the storage tank with coking tail gas;

(2) discharging the coking tail gas of the storage tank into a buffer tank for gas-liquid separation of the coking tail gas, and cooling preliminary dehydration, denaphthalene and detar in the buffer tank;

(3) The coking tail gas is sucked from the buffer tank to the Venturi mixer for removing impurities from the coking tail gas by the tail gas fan, and the hydrogen addition source is introduced into the Venturi mixer, and the hydrogen addition source and the coking tail gas are in the venturi fully mixed in the inner mixer, and the hydrogen content of the hydrogenation source is 30% to 60%;

(4) The gas mixed in the venturi mixer is discharged into the deoxygenation tank for catalytic hydrodeoxygenation, the deoxidation reaction temperature is from normal temperature to 300°C, and the air velocity of the mixed gas discharged into the deoxygenation tank is 5000～10000h-1;

(5) Carry out oxygen content detection on the deoxidized coking tail gas, if the oxygen content of the coking tail gas is less than 0.5%, the test is deemed qualified; Post exhaust gas treatment system.

Further, it also includes the step of collecting and discharging the coking tail gas of the tar ammonia water separation tank that is not easy to seal and discharges it into the buffer tank; 400Pa.

Further, it also includes the step of mixing the loading tail gas with the coking tail gas in the storage tank and collecting them into the buffer tank to ensure the air pressure balance in the buffer tank.

Further, in the step (3), the inlet pressure of the exhaust fan is 500-1500 Pa, and the outlet pressure of the exhaust fan is 0.1-0.5 MPa, so as to achieve the purpose of fire and explosion prevention.

Further, the hydrogenation source described in the step (3) is the clean gas that has been processed by the adsorption tower for dehydration and the desulfurization tower in turn, and the clean gas is passed through the tail gas in the deoxygenation tank described in the step (4). The coking tail gas extracted by the fan is reused.

Further, the present invention also provides a device adopting the above-mentioned coking tail gas treatment method, comprising at least one storage tank and a buffer tank, a Venturi mixer, and a deoxygenation tank which are sequentially communicated with the storage tank; The top of the storage tank is connected, a nitrogen filling valve is arranged on the nitrogen pipeline, and a quick release valve is arranged on the top of the storage tank; the coking tail gas in the storage tank is merged into the tail gas collection main pipe through the tail gas collection branch pipe, and the tail gas collection branch pipe The flame arrester one-way valve and one-way valve are arranged in sequence, and the flame arrester one-way valve is also arranged on the top of the storage tank;

The exhaust gas collection main pipe is connected with the air inlet at the top of the buffer tank, a heat exchanger is arranged in the buffer tank, the liquid outlet at the bottom of the buffer tank is connected with the water sealing tank; the air outlet of the buffer tank is connected with the Venturi mixer through the exhaust fan The gas inlet of the venturi mixer is connected to the hydrogenation device that provides the hydrogen gas source, and the gas outlet of the venturi mixer is connected to the gas inlet of the deoxygenation tank, and the gas outlet of the deoxygenation tank passes through The gas fan is communicated with the gas main.

Further, the hydrogenation device comprises an adsorption tower and a desulfurization tower connected in sequence, the deoxidation tank is communicated with the air inlet of the adsorption tower through a gas blower, and the air outlet of the desulfurization tower is connected to the hydrogenation of the venturi mixer. The air inlets are connected, and regulating valves are provided on the gas outlet pipelines of the adsorption tower and the desulfurization tower.

Further, it also includes a loading and unloading vehicle platform, and the loading tail gas balance pipe of the loading and unloading vehicle platform is communicated with the buffer tank through the tail gas collecting main pipe.

Further, it also includes that the tar ammonia water separation tank that is not easy to seal is also communicated with the buffer tank through a pipeline.

Further, the deoxygenation tank is an upright circular adiabatic reaction tank, the tank body is provided with at least a section of deoxygenation catalytic bed, the deoxygenation catalytic bed is set at a height of 1-3 meters, and the deoxygenation catalytic bed is equipped with a column or spherical deoxygenation. The catalyst, the deoxygenation catalyst is: palladium-based catalyst.

Compared with the prior art, the present invention has the following beneficial technical effects: the coking tail gas treatment method and device provided by the present invention realize the airtight collection of the coking tail gas, avoid the unorganized discharge of the coking tail gas, and ensure that the storage tank meets the requirements after being sealed. Relevant specifications for oil and gas collection in petrochemical systems and avoidance of storage tank extraction or bursting during operation, meet the requirements of the Ministry of Environmental Protection for the treatment of unorganized tail gas emissions in areas or workshops such as coking gas purification, so that tail gas emissions meet environmental protection requirements; at the same time effectively solve the problem. The problem of high oxygen content of gas in the gas purification system of the coking plant avoids the problem of frequent shutdown due to the high oxygen content of the gas, and reduces the hidden danger of gas explosion. The present invention performs hydrodeoxygenation on the collected coking tail gas with high oxygen content (oxygen content is 1-8%), so that oxygen and hydrogen in the coking tail gas react to generate water, thereby reducing the oxygen content (oxygen content) in the coking tail gas At 0.1 to 0.5%), the coking tail gas can directly enter the gas purification system of the coking plant for further purification treatment, thereby reducing the investment in tail gas post-treatment equipment.

Description of drawings

Fig. 1 is the structural representation of a kind of coking tail gas treatment device provided by the present invention;

Fig. 2 is another structural schematic diagram of a coking tail gas treatment device provided by the present invention.

Among them, 1. Nitrogen filling valve, 2. Storage tank, 3. Quick relief valve, 4. Flame arrester one-way valve, 5. One-way valve, 6. Exhaust gas collection branch pipe, 7. Exhaust gas collection main pipe, 8. Loading Exhaust balance pipe, 9. Loading oil pipe, 10. Oil tanker, 11. Buffer tank, 12. Regulating valve, 13. Venturi mixer, 15. Gas blower, 16. Deoxygenation tank, 17. Gas main pipe, 19. Water sealing tank, 20. Heat exchanger, 22. Cooling tower, 23. Exhaust fan, 24. Adsorption tower, 25. Desulfurization tower, 26. Tar ammonia water separation tank.

Detailed ways

The principles and features of the present invention will be described below with reference to the accompanying drawings and embodiments. The embodiments are only used to explain the present invention, but do not limit the scope of the present invention.

Specific examples are given below.

Embodiment 1: as shown in Figure 1, a kind of coking tail gas treatment method, comprises the following steps:

(1) The storage tank 2 storing the coking tail gas is sealed or filled with nitrogen;

(2) the coking tail gas of storage tank 2 is discharged into the buffer tank 11 for gas-liquid separation of the coking tail gas, and in the buffer tank 11, cooling preliminary dehydration, de-naphthalene and detarring;

(3) adopt the tail gas fan 23 to suck the coking tail gas from the buffer tank 11 to the Venturi mixer 13 for removing impurities from the coking tail gas, and feed the hydrogen addition source to the Venturi mixer 13, and the hydrogen addition source and the Venturi mixer 13 The coking tail gas is fully mixed in the venturi mixer 13, and the hydrogen content of the hydrogenation source is 30% to 60%;

(4) The gas mixed in the venturi mixer 13 is discharged into the deoxygenation tank 16 for catalytic hydrodeoxygenation, the deoxidation reaction temperature is from normal temperature to 300°C, and the air velocity of the mixed gas discharged into the deoxygenation tank 16 is 5000～10000h ^-1 ;

(5) The oxygen content of the deoxidized coking tail gas is detected, and the coking tail gas is regarded as qualified when the oxygen content is less than 0.5%; Enter the tail gas treatment system in the later stage, and the tail gas treatment system in the later stage adopts conventional oil and gas purification technologies, such as condensation, absorption, adsorption, membrane separation and other technologies.

Specifically, the hydrogenation source described in the step (3) is the clean gas that has been sequentially processed by the adsorption tower 24 for dehydration and the desulfurization tower 25, and the clean gas is obtained from the deoxygenation tank 16 described in the step (4). The recycled coking gas extracted by the gas blower 15 in the middle. The adsorption tower 24 can use an activated carbon adsorption tower, and the desulfurization tower 25 can use a zinc oxide fine desulfurization tower. The adsorption tower 24, the desulfurization tower 25 and the deoxygenation tank 16 are all existing equipment.

Further, in the step (3), the inlet pressure of the exhaust fan 23 is 500-1500 Pa, and the outlet pressure of the exhaust fan 23 is 0.1-0.5 MPa, so as to achieve the purpose of fire prevention and explosion protection.

It should be noted that the clean gas of the coking plant can also be used, and its hydrogen content is 50%. As a source of hydrogen, the condensate in the clean gas is treated by the adsorption tower 24 and the desulfurization tower 25. and hydrogen sulfide removal.

Embodiment 2: as shown in Figure 2, same as Embodiment 1, the difference is the described coking tail gas treatment method, also comprises the coking tail gas of the tar ammonia water separation tank 26 that is not easy to seal and is discharged into the buffer tank 11. Step; carry out micro-positive pressure nitrogen filling treatment to the tar ammonia water separation tank 26 that is not easy to seal, and the nitrogen filling pressure is 0-400Pa higher than atmospheric pressure.

At the same time, it also includes the step of mixing the loading exhaust gas and the coking exhaust gas in the storage tank 2 and collecting them into the buffer tank 11 together to ensure the air pressure balance in the buffer tank 11 . That is, while collecting the coking tail gas of the storage tank 2 to the buffer tank 11, the loading tail gas is collected to the buffer tank 11 and mixed with the coking tail gas of the storage tank 2, and the loading tail gas is discharged into the buffer tank through the loading tail gas balance pipe 8. In 11, the step of equilibrating the air pressure in the buffer tank 11.

Embodiment 3, as shown in FIG. 2 , the present invention also provides a device using the coking tail gas treatment method described in Embodiments 1 and 2, a coking tail gas treatment device, comprising at least one storage tank 2 and the storage tank. 2. The buffer tank 11, the Venturi mixer 13, the deoxygenation tank 16 communicated in turn, the nitrogen pipeline is communicated with the top of the storage tank 2, the nitrogen pipeline is provided with a nitrogen filling valve 1, and the top of the storage tank 2 is provided with a quick drain. The discharge valve 3; the coking tail gas in the storage tank 2 is merged into the tail gas collection main pipe 7 through the tail gas collection branch pipe 6, and the flame arrester single exhalation valve 4 and the one-way valve 5 are sequentially arranged on the tail gas collection branch pipe 6, and the flame arrester single exhalation The valve 4 is also arranged on the top of the storage tank 2;

The exhaust gas collection manifold 7 is communicated with the air inlet at the top of the buffer tank 11, a heat exchanger 20 is arranged in the buffer tank 11, the liquid outlet at the bottom of the buffer tank 11 is communicated with the water sealing tank 19; the air outlet of the buffer tank 11 passes through The exhaust fan 23 is communicated with the air inlet of the Venturi mixer 13, the hydrogenation device providing the hydrogenation source is communicated with the hydrogenation air inlet of the Venturi mixer 13, and the air outlet of the Venturi mixer 13 is connected with the deoxygenation tank 16. The air inlet of the deoxygenation tank 16 is communicated with the gas main pipe 17 through the gas fan 15 .

Specifically, the hydrogenation device includes an adsorption tower 24 and a desulfurization tower 25 that are connected in sequence, the deoxygenation tank 16 is communicated with the air inlet of the adsorption tower 24 through the gas fan 15, and the air outlet of the desulfurization tower 25 is connected to the venturi The hydrogenation gas inlet of the inner mixer 13 is connected, and a regulating valve 12 is provided on the gas outlet pipelines of the adsorption tower 24 and the desulfurization tower 25. The adsorption tower 24 can be an activated carbon adsorption tower, and the desulfurization tower 25 can be a zinc oxide fine desulfurization tower.

It should be noted that, in order to reduce the oxygen content in the collected exhaust gas, the storage tank 2 is sealed or filled with nitrogen. In order to meet the relevant fire protection regulations and avoid damage caused by misoperation of the storage tank 2, a quick relief valve 3, a flame arrester single-exhalation valve 4 with a flame arrester, a nitrogen filling valve 1 and an exhaust gas collection pipeline are installed on the top of the tank. Close the release valve on the top of the storage tank 2, and set up a nitrogen filling valve 1, a quick release valve 3 and a single-breathing valve 4 for the flame arrester on the top of the storage tank 2, wherein the single-breathing valve 4 for the flame arrester is a single-breathing valve with a flame arrester , a check valve 5 is set on the tail gas collection branch pipe 6, and a quick relief valve 3 and a flame arrester are set on the tail gas collection main pipe 7 to ensure that the tail gas collection system and the tail gas treatment system meet the relevant fire protection regulations.

Specifically, in order to equalize the pressure of the gas collection system, a buffer tank 11 is set so that the collected tail gas is initially condensed and cooled in the buffer tank 11 to achieve preliminary dehydration, naphthalene removal, and detar removal; the air inlet of the buffer tank 11 is communicated with the tail gas collection header 7 , the liquid outlet at the bottom of the buffer tank 11 is communicated with the water seal tank 19, and the water seal tank 19 performs gas-liquid separation and has an explosion-proof effect; a heat exchanger 20 is arranged in the buffer tank 11, and the heat exchanger 20 can use a coil. The heat exchanger is used to condense and cool the collected coking tail gas. It is usually cooled by cooling water and heated by steam to remove naphthalene during maintenance. A tail gas outlet is arranged in the middle and lower part of the buffer tank 11 to communicate with the air inlet of the tail gas fan 23, and a flame arrester, a regulating valve and a one-way valve can also be set on the connecting pipe of the buffer tank 11 and the tail gas fan 23 to ensure the tail gas collection system and the tail gas treatment system. Comply with relevant fire codes.

It also includes a loading and unloading vehicle platform, and the loading exhaust gas balance pipe 8 of the loading and unloading vehicle platform is communicated with the buffer tank 11 through the exhaust gas collecting main pipe 7 . The loading and unloading platform includes a fuel tanker 10 , and the loading exhaust gas balance pipe 8 of the fuel tanker 10 communicates with the buffer tank 11 through the exhaust gas collection manifold 7 . The loading and unloading platform adopts the steam balance method to discharge the loading exhaust gas into the buffer tank 11 through the loading exhaust gas balance pipe 8 , and the loading oil pipe 9 is connected to the oil tanker 10 by a quick sealing joint. It also includes that the tar ammonia water separation tank 26 which is not easy to seal is also communicated with the buffer tank 11 through pipelines.

The deoxygenation tank 16 is an upright circular adiabatic reaction tank. The deoxygenation tank 16 is provided with at least a section of a deoxygenation catalyst bed. The deoxygenation catalyst bed is set at a height of 1-3 meters. The deoxygenation catalyst bed is filled with a cylindrical or spherical shape. Deoxygenation catalyst, deoxygenation catalyst is: palladium-based catalyst.

Due to the large number ^of storage tanks in the coking plant and the different properties of the stored materials, there are many types of storage _tanks , and the volume of the storage tanks is different. Nitrogen sealing, the storage tank is reinforced after nitrogen sealing, and at the same time, fixing bolts are added to avoid deformation of the storage tank; for some smaller storage tanks, such as intermediate tanks and water sealing tanks, the release of the top of the tank is closed, and the implementation of The multiple tanks are connected and connected to the buffer tank 11 through a branch pipe; for the tar ammonia water separation tank 26 that is not easy to be filled with nitrogen and sealed, a slight positive pressure operation of nitrogen filling is performed to avoid air inhalation.

From the above technical solutions, the present invention provides a coking tail gas treatment method and device, by sealing or nitrogen-filling the storage tank 2 storing the coking tail gas; In the buffer tank 11 of liquid separation, and in the buffer tank 11, the preliminary dehydration, naphthalene removal and detar removal are cooled; the tail gas fan 23 is used to suck the coking tail gas from the buffer tank 11 to the Venturi mixer 13 for removing impurities from the coking tail gas. , and feed the hydrogen source to the venturi mixer 13, and the hydrogen source and the coking tail gas are fully mixed in the venturi mixer 13; the gas mixed in the venturi mixer 13 is discharged into the deoxygenation tank 16 for Catalytic hydrodeoxygenation; the oxygen content of the deoxidized coking tail gas is detected, if the oxygen content of the coking tail gas is less than 0.5%, the test is deemed qualified; the qualified coking tail gas is discharged into the gas main pipe 17 of the gas purification system of the coking plant, Or discharged into the later exhaust gas treatment system.

At the same time, the coking tail gas treatment method and device provided by the present invention realize the closed collection of the coking tail gas, avoid the unorganized discharge of the coking tail gas, and ensure that the storage tank complies with the relevant specifications for oil and gas collection in the petrochemical system after the storage tank is sealed, and avoids the occurrence of storage tanks in the operation process. The grate is pumped or burst to meet the requirements of the Ministry of Environmental Protection for the treatment of unorganized tail gas emissions from areas or workshops such as coking gas purification, so that the tail gas discharge meets the environmental protection requirements; at the same time, it effectively solves the problem of excessive oxygen content in the gas purification system of the coking plant, avoiding the need for It solves the problem of frequent parking due to the high oxygen content of the gas, and reduces the hidden danger of gas explosion.

The above are only preferred embodiments of the present invention and are not intended to limit the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection of the present invention. within the range.

Claims (9)

1. A coking tail gas treatment method is characterized by comprising the following steps:

(1) sealing or filling nitrogen to the storage tank storing the coking tail gas;

(2) discharging the coking tail gas of the storage tank into a buffer tank for gas-liquid separation of the coking tail gas, and cooling in the buffer tank for preliminary dehydration, naphthalene removal and tar removal;

(3) pumping the coking tail gas from the buffer tank to a Venturi mixer for removing impurities from the coking tail gas by adopting a tail gas fan, and introducing a hydrogenation gas source into the Venturi mixer, wherein the hydrogenation gas source and the coking tail gas are fully mixed in the Venturi mixer, and the hydrogen content of the hydrogenation gas source is 30-60%;

(4) discharging the gas mixed in the Venturi mixer into a deoxygenation tank for catalytic hydrodeoxygenation, wherein the deoxygenation reaction temperature is normal temperature to 300 ℃, and the space velocity of the mixed gas discharged into the deoxygenation tank is 5000-10000 h^-1；

(5) Detecting the oxygen content of the deoxidized coking tail gas, wherein the coking tail gas is qualified when the oxygen content of the coking tail gas is less than 0.5%; discharging qualified coking tail gas into a gas main pipe of a gas purification system of a coking plant or a tail gas treatment system at the later stage,

wherein, the hydrogenation gas source in the step (3) is clean coal gas which is treated by an adsorption tower and a desulfurizing tower for dehydration in sequence.

2. The coking tail gas treatment method according to claim 1, characterized by further comprising the step of collecting and discharging coking tail gas of the tar ammonia water separation tank which is difficult to seal into a buffer tank; the tar ammonia water separation tank which is difficult to seal is subjected to micro-positive pressure nitrogen charging treatment, and the nitrogen charging pressure is 0-400Pa higher than the atmospheric pressure.

3. The coking tail gas treatment method according to claim 1, characterized by further comprising the step of mixing the loading tail gas with the coking tail gas of the storage tank and collecting the mixture to the buffer tank to ensure the pressure balance in the buffer tank.

4. The coking tail gas treatment method according to claim 1, characterized in that in the step (3), the inlet pressure of the tail gas fan is 500-1500 Pa, and the outlet pressure of the tail gas fan is 0.1-0.5 MPa, so that the purposes of fire prevention and explosion prevention are achieved.

5. The coking tail gas treatment method according to any one of claims 1 to 4, characterized in that the clean gas is the recycled coking tail gas extracted from the deoxygenating tank in the step (4) through a tail gas fan.

6. The device for treating the coking tail gas according to any one of claims 1 to 5, which is characterized by comprising at least one storage tank, and a buffer tank, a Venturi mixer and a deoxidizing tank which are sequentially communicated with the storage tank; the nitrogen pipeline is communicated with the top of the storage tank, a nitrogen charging valve is arranged on the nitrogen pipeline, and a quick release valve is arranged on the top of the storage tank; coking tail gas in the storage tank is converged into a tail gas collecting main pipe through a tail gas collecting branch pipe, a flame arrester single-breathing valve and a one-way valve are sequentially arranged on the tail gas collecting branch pipe, and the flame arrester single-breathing valve is also arranged at the top of the storage tank;

the tail gas collecting main pipe is communicated with a gas inlet at the top of the buffer tank, a heat exchanger is arranged in the buffer tank, and a liquid outlet at the bottom of the buffer tank is communicated with the water seal tank; the gas outlet of the buffer tank is communicated with the gas inlet of the Venturi mixer through a tail gas fan, a hydrogenation device for providing a hydrogenation gas source is communicated with the hydrogenation gas inlet of the Venturi mixer, the gas outlet of the Venturi mixer is communicated with the gas inlet of the deoxygenation tank, the gas outlet of the deoxygenation tank is communicated with the gas main pipe through a gas fan,

hydrogenation equipment including the adsorption tower and the desulfurizing tower that communicate in proper order, the deoxidation jar be linked together through the air inlet of coal gas fan with the adsorption tower, the gas outlet of desulfurizing tower and the hydrogenation air inlet intercommunication of venturi mixer all are equipped with the governing valve on the outlet duct way of adsorption tower and desulfurizing tower.

7. The device of claim 6, further comprising a loading platform, wherein a loading tail gas balance pipe of the loading platform is communicated with the buffer tank through the tail gas collecting main pipe.

8. The device of claim 6, further comprising a tar-ammonia separation tank which is difficult to seal and is also communicated with the buffer tank through a pipeline.

9. The device of claim 6, wherein the deoxygenation tank is a vertical round adiabatic reaction tank, at least one section of deoxygenation catalyst bed is arranged in the tank body, the height of the deoxygenation catalyst bed is 1-3 m, a cylindrical or spherical deoxygenation catalyst is filled in the deoxygenation catalyst bed, and the deoxygenation catalyst is: a palladium-based catalyst.

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