CN101310827B - Activated charcoal gas cleaning method and device thereof - Google Patents

Abstract

The invention provides an activated coke gas purification method and device thereof, which have high desulfurization, high denitrification efficiency, energy saving, low bed resistance, high space utilization rate in an absorption tower, and low construction cost. The device comprises a total feed inlet at the upper part of the absorption tower, a total gas outlet, a total discharge port at the bottom of the absorption tower, a total gas inlet, and an activated coke bed located in the absorption tower. The activated coke bed is inclined, It forms an angle α with the vertical line. The steps of the method are as follows: the gas enters the activated coke bed through the gas inlet, and the gas flows from the bottom to the top in the inclined bed; at the same time, the activated coke enters the activated coke bed through the main inlet, and the gas flows in the inclined bed. The activated coke in the layer flows from top to bottom; after sufficient oblique convective contact is formed between the gas and the activated coke, the gas is discharged from the gas outlet, and the saturated activated coke is discharged from the outlet.

Description

A method and device for purifying activated coke gas

technical field

The invention relates to an activated coke gas purification method and device.

Background technique

Activated coke dry desulfurization and denitrification technology is often used in the purification of flue gas from industrial coal-fired boilers, and also in the purification of gas in absorption towers in the fields of chemical industry, metallurgy, glass, and pharmaceuticals.

<Development of Activated Coke Desulfurization Technology>

Activated coke desulfurization technology was developed in the 1960s. It is a dry desulfurization and denitrification technology based on the principle of physical-chemical adsorption. It has the advantages of large adsorption capacity, fast adsorption process and catalytic conversion. Activated coke that has adsorbed sulfur dioxide can be reused after regeneration, and the regenerated sulfur dioxide can also be made into by-products such as sulfuric acid, liquid sulfur dioxide or elemental sulfur. In Europe, America, Japan and other countries, this technology has been commercialized in many fields after years of research. The activated coke adsorption method was developed by the German BF company in 1967, and then Japan Mitsui Sumitomo introduced this technology (the scheme is Cross-flow absorption technology), WKV company, which evolved from German BF company, improved the shortcomings of cross-flow technology and invented the current international mainstream convection absorption technology.

<Working principle of activated coke desulfurization technology>

Activated coke is a carbon-based adsorbent with the characteristics of activated carbon. That is, activated coke itself is not only an adsorbent, but also a catalyst, and can also be used as a catalyst carrier. When the flue gas passes through the activated coke adsorption tower, SO ₂ , NO _X , O ₂ , H ₂ O in the flue gas and NH ₃ fed in are adsorbed in the pores of the active coke. Under the catalysis of active coke, SO ₂ reacts with O ₂ and H ₂ O, and finally attaches in the pores of active coke in the form of H ₂ SO ₄ ; NO reacts with O ₂ and NH ₃ to form N ₂ , and NO ₂ and NH ₃ The reaction produces N ₂ , so as to achieve the purpose of removing SO ₂ and NO _X in the coal-fired flue gas.

<Current Two Forms of Activated Coke Desulfurization Technology>

At present, there are two forms of activated coke dry flue gas desulfurization and denitrification technology: one is cross-flow adsorption technology, and the other is convective flow adsorption technology. The adsorption principle of the two technologies is as follows:

Fig. 1 is the structural schematic diagram of cross-flow adsorption technology, the top of the absorption tower is provided with fresh adsorbent inlet 24, the bottom of the absorption tower is provided with the adsorbent outlet 25 of adsorption saturation, the left side of the absorption tower is provided with gas inlet 26, and the right side of the absorption tower is provided with There is a gas outlet 27 . As shown in the figure, the adsorbent in the absorption tower can be divided into three regions, the adsorbent with high adsorption saturation in the region 28 near the gas inlet 26 side; near the gas outlet 27 side, and fresh adsorption The area 29 near the agent inlet 24 is relatively fresh adsorbent; the area 30 near the lower part of the absorption tower is the adsorbent saturated with adsorption.

The development of cross-flow adsorption technology is relatively early. The gas passes through the absorption tower from left to right on the side of the absorption tower, and the active coke passes through the absorption tower from top to bottom, and the two are in cross-flow contact. The advantages are: large air intake area, low gas velocity in the tower, and small bed resistance. Since there is no need for air intake, air outlet space, active coke storage and feeding space in the tower, the space utilization rate in the absorption tower is large. Disadvantages: The flue gas enters the activated coke bed from the side, the activated coke near the flue gas inlet first undergoes adsorption reaction and reaches saturation first, the flue gas moves from left to right, the adsorption saturation of activated coke decreases in turn, the overall distribution The adsorption saturation of activated coke decreases from left to right, and increases from top to bottom. The adsorption of activated coke on the side near the flue gas outlet is less, so that some of the activated coke discharged is not fully adsorbed. In this way, part of the fresh active coke is discharged and sent for regeneration, so that the circulation of active coke is increased, and the increase of circulation also increases the power consumption and damage, and the amount of regeneration gas increases, resulting in Energy is wasted. In addition, due to the large saturation of the activated coke in the lower part, the desulfurization efficiency is low. The upper active coke is relatively fresh, so the desulfurization efficiency is higher, and the total desulfurization and denitrification efficiency of the gas outlet is the average of the efficiencies of the upper and lower positions. value, so its desulfurization and denitrification efficiency is not as high as that of convective adsorption.

Figure 2 is a schematic diagram of the structure of the convective adsorption technology. The top of the absorption tower is provided with a fresh adsorbent inlet 24, the bottom of the absorption tower is provided with an adsorbent discharge port 39 after adsorption saturation, the lower part of the absorption tower is provided with a gas inlet 26, the upper part of the absorption tower is provided with a gas outlet 27, and the absorption tower is provided with Adsorbent bed 33. The equipment shown in the figure also includes: activated coke adsorbent storage bin 31, adsorbent uniform distribution device 32, adsorbent outlet and gas inlet distributor 34, adsorbent feeding device 35, gas inlet sealing partition 36 , a discharge controller 37, a discharge storage bin 38.

The convective adsorption technology is to let the flue gas pass through the active coke bed evenly from the bottom up, and the fresh active coke flows down from the top to contact with the gas convection, so that the adsorption saturation of the active coke in the bed decreases from bottom to top. , the activated coke saturated with adsorption is discharged first, and the adsorption capacity of the activated coke on the same plane is the same, so the rate of decline of the activated coke is almost the same, so that the utilization rate of the activated coke is greatly improved, and because the bed The thickness of the layer is uniform, the flue gas intake is also uniform, the resistance of each point of the flue gas is also uniform, and the contact time between the flue gas and the activated coke is basically the same. The higher, the highest can reach more than 99%. In terms of the circulating amount of active coke, since the feeding amount of each point in the tower is the same in the convection technology, the active coke particles at the outlet of the tower are almost saturated, that is to say, the same amount of SO ₂ is adsorbed, and the active coke used in the convection technology The coke is relatively less, and the active coke discharged is less, that is, the circulation volume is small, and the system is more energy-saving. The disadvantages are: because the flue gas enters the absorption tower at the bottom, the air intake area is small, the air velocity in the tower is high, and the bed resistance is large. , Active coke lower silo, so the space utilization rate in the convective absorption tower is low.

Convective adsorption technology is an adsorption technology developed after cross-flow adsorption technology. Its advantages are high adsorption efficiency and high utilization of activated carbon; its disadvantages are complex construction process and high construction cost. Since the active coke bed layer using convective adsorption technology is mostly planar, it occupies a large area and requires more steel and other materials during construction; since the adsorption surface is flat, multiple valves and pipelines need to be installed in the active coke recovery part. The structure is complex, the amount of steel used is large, and it is also prone to failure. Generally, under the same flue gas treatment capacity, the construction cost of the convective adsorption technology is about twice that of the cross-flow adsorption technology. For example, to build an adsorption equipment with an adsorption capacity of 2.2 million standard cubic flue gas, the construction cost of using convective adsorption technology is about 420 million yuan, and the construction cost of using cross-flow adsorption technology is about 208 million yuan.

【 Content of invention 】

The technical problem to be solved by the present invention is to provide a method and device for purifying activated coke gas with high desulfurization and denitrification efficiency, energy saving, low bed resistance, high space utilization rate in the absorption tower, and low construction cost.

In order to solve the problems of the technologies described above, the present invention adopts the following technical solutions:

An activated coke gas purification device, comprising a total feed inlet at the upper part of the absorption tower, a total gas outlet, a total discharge port at the lower part of the absorption tower, a total gas inlet, and an activated coke bed located in the absorption tower. The activated coke bed is inclined, forming an angle α between it and the vertical line of the horizontal plane. The activated coke bed is divided into a plurality of inclined unit activated coke beds through laminar flow partitions. A unit gas inlet is arranged below the unit activated coke bed, and an inlet gas passage is arranged between the unit gas inlet and the gas total inlet; a unit gas outlet is arranged above the unit activated coke bed, and the unit gas outlet is arranged above the unit activated coke bed. An outlet gas channel is provided between the gas outlet and the total gas outlet; a unit feed port is arranged above the unit activated coke bed, and the unit feed port is connected to the total feed port through a unit feed port channel; A unit discharge port is arranged below the unit activated coke bed, and the unit discharge port is connected to the general discharge port through a channel of the unit discharge port.

Further, a storage bin is arranged between the unit feed port channel and the general feed port.

Further, a unit feed port is provided above the unit activated coke bed, and the unit feed port is connected to the main feed channel through the unit feed port channel, and the main feed channel is connected to the general feed port.

Further, a storage bin is arranged between the main feeding port channel and the main feeding port.

Further, a unit discharge port is arranged below the unit activated coke bed, and the plurality of unit discharge ports can be divided into several groups, and each group of unit discharge ports passes through the unit discharge port channel and the primary discharge channel. The multiple primary discharge channels are connected to the total discharge port through the secondary discharge channels.

Further, according to the number of unit activated coke beds, a tertiary discharge channel or more than three discharge channels are set between the secondary discharge channel and the total discharge port.

Further, the vertical distance between the upper and lower bottom surfaces of the unit activated coke bed is H, and the horizontal projection distance between the two sides where the unit air inlet of the unit activated coke bed and the unit gas outlet are located is L , the ratio range of the vertical distance H to the horizontal projection distance L is: 0.4≤H:L≤2.

Further, the range of the included angle α is: 35°≤α≤65°.

Further, the gas inlet of the unit is provided with an air inlet retaining device; the air inlet retaining device is at an angle of 45 degrees to the vertical direction of the horizontal plane, and the air inlet retaining device is composed of baffles located around the unit gas inlet.

Further, the gas outlet of the unit is provided with a gas outlet blocking device; the gas outlet blocking device is at an angle of 45 degrees to the vertical direction of the horizontal plane, and the gas outlet blocking device is composed of baffles located around the unit gas outlet. the

A method for purifying activated coke gas, wherein the activated coke bed in the absorption tower is set to be inclined, the top of the activated coke bed is provided with a total gas outlet, a total feed port, and the unit below the activated coke bed A total gas inlet and a total discharge port are provided, and the steps of the method are as follows:

The gas enters the activated coke bed through the gas inlet, and the gas flows from bottom to top in the inclined bed;

At the same time, the activated coke enters the activated coke bed through the total feed port, and the activated coke flows from top to bottom in the inclined bed;

After sufficient oblique convective contact is formed between the gas and the activated coke, the gas is discharged from the gas outlet, and the activated coke after adsorption saturation is discharged from the outlet.

Further, the activated coke bed is separated into a plurality of inclined unit activated coke beds with a laminar flow partition, and a unit gas outlet and a unit feed port are arranged above the unit activated coke bed, and the unit activated coke bed The lower part of the layer is provided with a unit gas inlet and a unit outlet, and the steps of the method are as follows:

The gas enters the activated coke bed of each unit through the unit inlet, and the gas flows from bottom to top in the inclined unit bed;

At the same time, activated coke enters each unit activated coke bed through the unit feed port, and the activated coke flows from top to bottom in the inclined unit bed;

After sufficient oblique convective contact is formed between the gas and activated coke, the gas is discharged from the gas outlet of the unit, and the activated coke after adsorption saturation is discharged from the outlet of the unit.

The invention adopts the laminar flow adsorption technology, and compared with the cross-flow adsorption technology, the adsorption efficiency of the technical solution in the invention is obviously improved, but the construction cost is not much different. Compared with the convective adsorption technology, under the same adsorption efficiency, the construction cost of the technical solution in the present invention is only about half of that of the convective adsorption technology, and it saves steel, has high space utilization rate, and saves floor area. For example, to build an adsorption device with an adsorption capacity of 2.2 million standard cubic flue gas, the construction cost of adopting convective adsorption technology is about 420 million yuan, and the construction cost of adopting the technical solution of the present invention is about 300 million yuan, which can save 120 million yuan , saving about 30% of the cost.

The gas to be purified in the present invention can be flue gas produced by industrial coal combustion, or other gases that need to be purified.

The beneficial effects of the present invention are:

At the same time, it has the advantages of convective adsorption technology and cross-flow adsorption technology, high desulfurization and denitrification efficiency, small bed resistance, large absorption saturation of activated coke, small circulation volume and small loss, low regeneration energy consumption, high space utilization rate in the absorption tower, Low construction cost.

Description of drawings

Figure 1 is a schematic diagram of the cross-flow adsorption technology structure;

Figure 2 is a schematic diagram of the convective adsorption technology structure;

Fig. 3 is a schematic structural view of Embodiment 1 of the present invention;

Fig. 4 is a left view along the direction A-A of Embodiment 1 of the present invention;

Fig. 5 is a right view along the B-B direction of Embodiment 1 of the present invention;

Fig. 6 is a schematic structural view of the air inlet stopper device according to Embodiment 1 of the present invention;

Fig. 7 is a schematic structural view of the air outlet blocking device according to Embodiment 1 of the present invention;

Fig. 8 is a schematic diagram of the proportion of a unit activated coke bed structure in the embodiment of the present invention;

Fig. 9 is a schematic diagram of the feed structure of Embodiment 2 of the present invention;

Fig. 10 is a schematic diagram of the discharge structure of Embodiment 3 of the present invention;

In the accompanying drawings, the list of parts represented by each label is as follows:

1. Unit inlet 2. Unit activated coke bed 3. Unit gas inlet 4. Unit outlet 5. Unit discharge port 6. Gas inlet 7. Inlet gas channel 8. Storage bin 9. Gas outlet 10. Unit gas outlet 11. Sealing plate 12. Laminar flow partition 13. Air outlet stopper device 14. Air inlet stopper device 15. Discharge port pusher 16. Total feed port 17. Unit feed port Channel 18, unit outlet channel 19, outlet gas channel 20, total outlet 21, main feed channel 22, primary discharge channel 23, secondary feed channel 24, fresh adsorbent inlet 25, adsorption saturated Adsorbent outlet 26, gas inlet 27, gas outlet 28, adsorbent with high adsorption saturation 29, relatively fresh adsorbent 30, saturated adsorbent 31, activated coke adsorbent storage bin 32, adsorbent uniform distribution device 33 , Adsorbent bed 34. Adsorbent outlet and gas inlet gas distributor 35. Adsorbent feeding device 36. Gas inlet sealing partition car 37. Discharge controller 38. Discharge storage bin 39. After adsorption saturation Adsorbent discharge port

Detailed ways

The principles and features of the present invention are described below in conjunction with the accompanying drawings, and the examples given are only used to explain the present invention, and are not intended to limit the scope of the present invention.

As shown in Figure 3, the top of the absorption tower is provided with a total feed port 16, and the bottom of the total feed port is provided with a storage bin 8, fresh activated coke is stored in the storage bin 8, and the upper part of the absorption tower is provided with a gas collector. Outlet 9, the bottom of the absorption tower is provided with a total discharge port 20 and a total gas inlet 6.

There is an activated coke bed in the absorption tower, the activated coke bed is inclined, and the activated coke bed is composed of a plurality of inclined unit activated coke beds 2, and each unit activated coke bed 2 is passed through a laminar flow partition 12 were separated. Each unit activated coke bed 2 is parallel to each other, and the angle between each unit activated coke bed 2 and the vertical line is 45°, and the angle α between the unit activated coke bed 2 and the vertical line can also be It is set to other angles in the range of 35°≤α≤65° to ensure that the activated coke can flow downward by gravity.

Uniformly distributed unit gas inlets 3 are arranged obliquely below the unit activated coke bed 2 , and an inlet gas channel 7 is provided between the unit gas inlet 3 and the total gas inlet 6 . The unit gas inlet 3 is located at the side of the absorption tower, and the flue gas enters the inlet gas channel 7 through the gas main inlet 6, and then enters the unit activated carbon bed 2 through the unit gas inlet 3 respectively. Uniformly distributed unit gas outlets 10 are arranged obliquely above the unit activated coke bed 2 , and an outlet gas channel 19 is provided between the unit gas outlet 10 and the gas main outlet 9 . The purified gas is collected in the outlet gas channel 19 and discharged from the gas outlet 9 .

A unit feed port 1 is arranged obliquely above the unit activated coke bed 2, and the unit feed port 1 is connected to the storage bin 8 located below the total feed port 16 through the unit feed port channel 17, or no storage is required. The warehouse, that is, the unit feed port is directly connected with the total feed port. A unit discharge port 4 is arranged obliquely below the unit activated coke bed 2, and the unit discharge port 4 is connected with the total discharge port 20 at the bottom of the absorption tower through the unit discharge port channel 18, and each unit discharge port channel The end of 18 is the unit discharge opening 5.

A discharge control device is arranged on the unit discharge port 5, namely the discharge port pusher 15, the discharge port pusher 15 is a discharge device, and the discharge amount is reduced when the discharge port pusher 15 moves fast. Less, when the movement is slow, the amount of feeding will be more, so as to control the amount of feeding at the discharge port 5 of the unit. When the discharge port pusher 15 stops directly below the unit discharge port 5, the unit discharge port 5 stops blanking. The discharge port pusher 15 can be used to control the uniform discharge of each unit activated coke bed 2, avoid blocking or bias flow, and control the discharge of each unit activated coke bed 2 according to the pushing speed of the discharge port pusher 15. The amount of material can be observed, so as to prevent the unit activated coke bed 2 from being unloaded due to blockage.

The sealing plate 11 is made of flat steel plates on the upper and lower sides of the absorption tower, and its size is the same as the length and width of the absorption tower. It plays the role of sealing flue gas and supporting the tower body.

As shown in Figure 4, a plurality of unit activated coke beds 2 are arranged side by side up and down, and a plurality of unit gas inlets 3 are arranged side by side on each unit activated coke bed 2, and a plurality of unit discharge port passages 18, unit gas inlets 3 and the unit outlet channel 18 in a staggered distribution.

As shown in Figure 5, a plurality of unit activated coke beds 2 are arranged side by side up and down, and a plurality of unit gas outlets 10 are arranged side by side on each unit activated coke bed 2, and a plurality of unit feed port passages 17, unit gas outlets 10 and the unit feed port channel 17 are distributed in a staggered manner.

As shown in FIG. 3 , the unit gas inlet 3 is provided with an air inlet stopper 14 , and the unit gas outlet 10 is provided with an air outlet stopper 13 .

As shown in Figure 6, the air inlet retaining device 14 is 45 degrees with the vertical direction, and the air inlet retaining device 14 is formed by a baffle plate positioned around the unit gas inlet 3, which surrounds the unit gas inlet 3 to carry out The gas port blocking device 14 can prevent activated coke from leaking at the unit gas inlet 3.

As shown in Figure 7, the gas outlet blocking device 13 is 45 degrees with the vertical direction, and the gas outlet blocking device 13 is composed of baffles positioned around the unit gas outlet 10, which surrounds the unit gas outlet 10, and the gas outlet blocking The feeding device 13 can prevent activated coke from leaking at the unit gas outlet 10.

As shown in Figure 8, the vertical distance between the upper and lower bottom surfaces of the unit activated coke bed is H, and the unit activated coke bed 2 is located at the horizontal projection distance between the two sides where the unit gas inlet 3 and the unit gas outlet 10 are located is L, the ratio range of the vertical distance H to the horizontal projection distance L is: 0.4≤H:L≤2.

As shown in Figure 3, the layered inclined unit activated coke bed structure is symmetrically distributed in the absorption tower.

When performing desulfurization and denitrification, the gas enters the activated coke bed 2 of each unit from the gas inlet 6 through the inlet gas passage 7, and then enters the activated coke bed 2 of each unit through the unit gas inlet 3, and the gas flows from obliquely below to obliquely above in the inclined bed; Fresh activated coke enters the storage bin 8 from the total feed port 16, and enters each unit activated coke bed 2 through the unit feed port channel 17 from the storage bin 8, and the activated coke flows from obliquely above to obliquely below; gas and After sufficient oblique convective contact is formed between the activated cokes, the purified gas is discharged from the unit gas outlet 10, and is concentrated in the outlet gas channel 19, and is discharged from the gas outlet 9; the saturated activated coke is discharged from the unit Port 4 is discharged, through the unit discharge port channel 18, and discharged from the total discharge port 20.

Embodiment two

As shown in Figure 9, the difference between this embodiment and Embodiment 1 is that the feed structure is set as follows: a unit feed port 1 is provided above the unit activated coke bed 2, and the unit feed port 1 passes through the unit The feeding port channel 17 is connected with a main feeding channel 21 , and the main feeding channel 21 is connected with the storage bin 8 located below the main feeding port 16 .

Embodiment Three

As shown in Figure 10, the difference between this embodiment and Embodiment 1 is that the discharge structure is set as follows: a unit discharge port 1 is provided below the unit activated coke bed 2, and a plurality of unit discharge ports 1 It can be divided into several groups, each group of unit outlets 1 is connected with the primary discharge channel 22 through the unit discharge channel 18, and the above-mentioned multiple primary discharge channels 22 are connected with the total discharge channel 23 through the secondary discharge channel 23. The feed port 20 is connected. According to the quantity of the unit activated coke bed, a tertiary discharge channel or more than three discharge channels can also be set between the secondary discharge channel 23 and the total discharge port 20 .

In each embodiment of the present invention, each unit activated coke bed is provided with an independent feed inlet and outlet to ensure the absorption efficiency of each absorption unit. In each unit of activated coke bed, activated coke flows from obliquely upward to obliquely downward, gas flows from obliquely downward to upward, countercurrent contact adsorption, and the adsorbent at the outlet of each unit reaches the adsorption saturation state. The gas adsorption efficiency of the gas outlets of each unit is the same, and the side air intake is adopted, the air intake area is larger, and the bed resistance is smaller. The present invention has the advantages of both countercurrent adsorption technology and cross-flow adsorption technology, high desulfurization and denitrification efficiency, small bed resistance, high absorption saturation of activated coke, small circulation volume, low loss, low regeneration energy consumption, and high space utilization rate in the tower , Low construction cost.

The above is only the embodiment of the present invention, and does not limit the patent scope of the present invention. All equivalent transformations made by using the description of the present invention and the contents of the accompanying drawings are directly or indirectly used in other related technical fields. included in the patent scope of the present invention.

Claims (10)

1. A kind of activated coke gas purifying device, comprise the total feed inlet that is positioned at absorption tower top, gas total outlet, the total discharge port of absorption tower bottom, gas total inlet, and be positioned at the activated coke bed layer in absorption tower, its It is characterized in that, the described activated coke bed is inclined, and forms an included angle α between it and the vertical line of the horizontal plane, and the described activated coke bed is divided into a plurality of inclined unit activated coke beds by laminar flow partitions layer, the unit gas inlet is arranged below the unit activated coke bed, and an inlet gas channel is arranged between the unit gas inlet and the gas total inlet; a unit gas outlet is arranged above the unit activated coke bed, so An outlet gas channel is provided between the unit gas outlet and the total gas outlet; a unit feed port is arranged above the unit activated coke bed, and the unit feed port communicates with the total feed port through the unit feed port channel Connection; a unit discharge port is provided below the unit activated coke bed, and the unit discharge port is connected to the general discharge port through a channel of the unit discharge port. 2. The activated coke gas purification device according to claim 1, characterized in that, a storage bin is arranged between the unit feed port channel and the general feed port. 3. activated coke gas purifying device according to claim 1, is characterized in that, the top of described unit activated coke bed is provided with unit feed port, and described unit feed port passes through unit feed port channel and main feed The feed channel is connected, and the main feed channel is connected with the total feed port. 4. The activated coke gas purification device according to claim 3, characterized in that, a storage bin is arranged between the main feed channel and the main feed port. 5. activated coke gas purification device according to claim 1, is characterized in that, the below of described unit activated coke bed is provided with unit outlet, and described multiple unit outlet can be divided into some groups, each The group unit discharge port is connected to the first-stage discharge channel through the unit discharge port channel, and the multiple primary discharge channels are connected to the general discharge port through the secondary discharge channel. 6. The activated coke gas purification device according to claim 5, characterized in that, according to the number of unit activated coke beds, a three-stage discharge channel or a three-stage discharge channel is set between the secondary discharge channel and the total discharge port. above the discharge channel. 7. activated coke gas purification device according to claim 1, is characterized in that, the vertical distance between the upper and lower bottom surfaces of the unit activated coke bed is H, and the unit air inlet of the unit activated coke bed The horizontal projection distance between the two sides where the air outlet of the unit is located is L, and the ratio range of the vertical distance H to the horizontal projection distance L is: 0.4≤H:L≤2. 8. The activated coke gas purification device according to claim 1, characterized in that, the range of the included angle α is: 35°≤α≤65°. 9. The activated coke gas purification device according to claim 1, characterized in that, said unit gas inlet is provided with an air inlet retaining device; the air inlet retaining device forms an angle of 45 degrees with the vertical direction of the horizontal plane, The gas inlet blocking device is composed of baffles located around the unit gas inlet. 10. The activated coke gas purification device according to claim 1, characterized in that, said unit gas outlet is provided with a gas outlet blocking device; the gas outlet blocking device forms an angle of 45 degrees with the vertical direction of the horizontal plane, and the gas outlet The blocking device consists of baffles located around the gas outlet of the unit.

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