CN113828109B - Flue gas purification system and its moving bed adsorption tower with distributor - Google Patents

Abstract

The invention discloses a flue gas purification system and a moving bed adsorption tower with a distributor, wherein the moving bed adsorption tower comprises a tower body, the distributor and a plurality of blanking pipes, a cavity is arranged in the tower body, the tower body is provided with a feed inlet, a discharge outlet, a flue gas inlet and a flue gas outlet which are communicated with the cavity, and the cavity is provided with an air inlet section, a filler section and a material distribution section in the flowing direction of flue gas; the distributor is arranged in the tower body and comprises a plurality of blanking inlets and a plurality of blanking outlets corresponding to the blanking inlets, and the distributor is positioned below the filling section, wherein the blanking inlets are square; the blanking pipes correspond to the blanking outlets one by one, the blanking outlets are positioned in the blanking pipes, a gap is reserved between each blanking pipe and the distributor, the smoke inlet is positioned below the blanking inlet, and the blanking pipes are positioned above the discharge outlet. The invention has the advantages of uniform adsorption and good adsorption effect.

Description

Flue gas purification system and its moving bed adsorption tower with distributor

technical field

The present application relates to the technical field of flue gas treatment, in particular to a flue gas purification system and a moving bed adsorption tower with a distributor.

Background technique

The large amount of pollutants produced by coal combustion flue gas is one of the important factors that endanger the atmospheric environment and human health. In the field of flue gas purification, fixed bed adsorption towers are usually used to adsorb pollutants in flue gas to achieve the purpose of purifying flue gas. The problem of unevenness, poor adsorption effect, and the decrease of adsorption capacity with the extension of use time, and the need to stop working when the adsorbent needs to be replaced, seriously affects the adsorption efficiency and increases the difficulty of operation. The related technology adopts the moving bed adsorption tower to make the adsorbent flow in the tower, so as to overcome the problem that the adsorption capacity of the fixed bed adsorption tower decreases with the prolongation of use time, but there are still uneven distribution of flue gas and poor purification effect in the moving bed adsorption tower. Ideal question.

Contents of the invention

The present invention aims to solve one of the technical problems in the related art at least to a certain extent. For this reason, the embodiment of the present invention proposes a moving bed adsorption tower, which has the advantages of uniform adsorption and good adsorption effect.

Embodiments of the present invention also provide a flue gas purification system comprising the above-mentioned moving bed adsorption tower.

The moving bed adsorption tower according to the embodiment of the present invention includes a tower body, the tower body has a cavity, and the tower body is provided with a feeding port, a material outlet, a flue gas inlet and a flue gas outlet communicating with the cavity , the cavity has an inlet section, a packing section and a cloth section in the flow direction of the flue gas, and the packing section is used to fill the adsorbent; the distributor, the distributor is arranged in the tower body, the distribution The device includes a plurality of blanking inlets and a plurality of blanking outlets corresponding to the blanking inlets, and the distributor is located below the packing section so that the adsorbent in the packing section passes through the blanking inlets and corresponding The blanking outlets flow out, wherein the blanking inlets are square; multiple blanking tubes correspond to multiple blanking outlets one by one, and the blanking outlets are located at the In the drop pipe, there is a gap between the drop pipe and the distributor for flue gas to pass through, the flue gas inlet is located below the drop inlet, and the drop pipe is located above the discharge port .

The moving bed adsorption tower according to the embodiment of the present invention has the advantages of uniform adsorption and good adsorption effect.

In some embodiments, the distributor includes a distribution plate and a plurality of distribution pipes, the blanking inlet is set on the distribution plate, the distribution pipe is connected to the lower end surface of the distribution plate and passes from the distribution plate The plate extends downwards, the distribution pipe is a square pipe, and a plurality of the distribution pipes correspond to a plurality of the blanking inlets, the lower end of the distribution pipe is provided with the blanking outlet, and the plurality of the falling The feeding pipe corresponds to a plurality of the distribution pipes one by one, the lower end of the distribution pipe extends into the upper end of the corresponding feeding pipe, and the top end of the feeding pipe and the lower end surface of the distribution plate There is a gap, there is a space between the distribution pipe and the corresponding drop pipe, and the smoke inlet is located below the distribution plate.

In some embodiments, the vertical dimension of the gap between the top end of the drop tube and the lower end surface of the distribution plate is 20mm-100mm.

In some embodiments, the distance between the outer peripheral wall of the distribution pipe and the corresponding inner peripheral wall of the drop pipe is 5mm-40mm in the horizontal direction.

In some embodiments, the length of the part of the distribution pipe protruding into the discharge pipe is 5mm-40mm

In some embodiments, the multiple blanking inlets are arranged in multiple rows, each row of blanking inlets includes several blanking inlets, and several blanking inlets in each row of blanking inlets are arranged at intervals along the first direction, Multiple rows of blanking inlets are arranged at intervals in the second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of blanking inlets are aligned in the second direction.

In some embodiments, the edge of the blanking inlet is square, and the side length of the blanking inlet is 150mm-300mm.

In some embodiments, the interval between two adjacent blanking inlets in the first direction is 20mm-100mm, and the interval between two adjacent blanking inlets in the second direction is 20mm-100mm.

In some embodiments, the feeding tube is a circular tube, and the feeding tube includes a first section and a second section, the diameter of the first section is larger than the diameter of the second section, and the first section The lower end of the distribution pipe is connected to the upper end of the second section, and the lower end of the distribution pipe extends into the corresponding first section of the drop pipe.

The flue gas purification system according to the embodiment of the present invention includes: a flue gas cooling device, the flue gas cooling device has a smoke inlet and a smoke outlet, and the flue gas cooling device is used to The flue gas is cooled to room temperature and below; a moving bed adsorption tower, the moving bed adsorption tower is the moving bed adsorption tower described in any one of the above embodiments, and the smoke outlet of the flue gas cooling device is adsorbed with the moving bed The flue gas outlet of the tower is connected, and the moving bed adsorption tower is used for adsorbing the flue gas.

Description of drawings

Fig. 1 is a front view of a moving bed adsorption tower according to an embodiment of the present invention.

Fig. 2 is a top view of a moving bed adsorption tower according to an embodiment of the present invention.

Fig. 3 is a cross-sectional view at A-A in Fig. 2 .

Fig. 4 is a cross-sectional view at B-B in Fig. 3 .

Fig. 5 is a front view of the distributor of Fig. 3 .

FIG. 6 is a schematic cross-sectional view of a plurality of drop tubes in FIG. 3 .

Fig. 7 is a schematic cross-sectional view of a plurality of drop tubes in another embodiment.

Reference signs:

Tower body 1; material distribution section 11; feeding port 111; packing section 12; flue gas outlet 121; air intake section 13; flue gas inlet 131; discharge section 14; discharge port 141;

Distributor 2; distribution plate 21; distribution pipe 22; blanking inlet 23; blanking outlet 24;

Falling tube 3; first section 31; second section 32.

Detailed ways

Embodiments of the invention are described in detail below, examples of which are illustrated in the accompanying drawings. The embodiments described below by referring to the figures are exemplary and are intended to explain the present invention and should not be construed as limiting the present invention.

As shown in FIGS. 1 to 3 , a moving bed adsorption tower according to an embodiment of the present invention includes a tower body 1 , a distributor 2 and a plurality of downcomers 3 .

There is a cavity in the tower body 1, and the tower body 1 is provided with a feed port 111, a discharge port 141, a flue gas inlet 131 and a flue gas outlet 121 communicating with the cavity, and the cavity has an inlet section in the flow direction of the flue gas 13. The packing section 12 and the cloth section 11, the packing section 12 is used for filling the adsorbent;

Specifically, the flue gas inlet 131 communicates with the air inlet section 13, the flue gas outlet 121 communicates with the material distribution section 11, the feeding port 111 communicates with the material distributing section 11, the feeding port 111 and the flue gas outlet 121 are located above the packing section 12, and the discharge The port 141 and the flue gas inlet 131 are located below the packing section 12 . It should be noted that the flue gas flow direction is from the flue gas inlet 131 to the flue gas outlet 121 , and the fabric section 11 , filler section 12 and air intake section 13 are arranged sequentially from top to bottom. Thus, the flue gas enters the interior of the tower body 1 from the lower half of the tower body 1 and flows out from the upper side of the tower body 1, and the adsorbent enters the tower body 1 from the upper side of the tower body 1 and flows out from the lower end of the tower body 1 , the flow direction of the flue gas is opposite to that of the adsorbent, the concentration of nitrogen and sulfur in the flue gas gradually decreases as the flue gas rises, the adsorption effect of the adsorbent gradually decreases with the contact time with the flue gas, and the lower nitrogen and sulfur concentrations The flue gas is contacted with an adsorbent with good adsorption effect, which can effectively reduce the concentration of nitrogen and sulfur in the gas discharged from the flue gas outlet 121, and improve the adsorption efficiency.

Distributor 2 is arranged in tower body 1, and distributor 2 comprises a plurality of blanking inlets 23 and a plurality of blanking outlets 24 corresponding to blanking inlets 23, and distributor 2 is positioned at the below of packing section 12 so that in packing section 12 The adsorbent flows out through the blanking inlet 23 and the corresponding blanking outlet 24, wherein the blanking inlet 23 is square;

Specifically, the blanking outlets 24 correspond to the blanking inlets 23 one by one, the blanking outlets 24 are located below the blanking inlets 23, and the blanking inlets 23 are arranged in parallel and at intervals with equal intervals. Thus, the adsorbent enters the drop pipe 3 through the blanking inlet 23 and the blanking outlet 24, and the flow rate of the adsorbent through the uniformly arranged blanking inlets 23 is approximately the same. On the one hand, the speed of the downward flow of the adsorbent is slowed down. The contact time between the adsorbent particles and the flue gas is increased, and on the other hand, it prevents the adsorbent from concentrating on flowing out from one or more distribution pipes 22, resulting in dead angles in the flow, and improves the flow efficiency of the adsorbent, thereby improving the adsorption effect.

Multiple blanking tubes 3 correspond to multiple blanking outlets 24 one by one, the blanking outlets 24 are located in the blanking tube 3, there is a gap between the blanking tube 3 and the distributor 2 for the passage of smoke, and the smoke inlet 131 is located at Below the blanking inlet 23 , the blanking pipe 3 is located above the material outlet 141 .

Specifically, the lower end of the blanking outlet 24 extends into the inside of the blanking tube 3, and the gap between the blanking tube 3 and the distributor 2 is the distance between the upper end of the inner wall of the blanking tube 3 and the lower end of the outer wall of the blanking outlet 24. void. Thus, when the adsorbent passes through the blanking outlet 24 and falls into the blanking tube 3, it can completely fall into the blanking tube 3, preventing the adsorbent from splashing out from the gap between the blanking outlet 24 and the blanking tube 3, This prevents the adsorbent from flowing out of the tower body 1 from the flue gas inlet 131 .

In some embodiments, the distributor 2 includes a distribution plate 21 and a plurality of distribution pipes 22, the blanking inlet 23 is arranged on the distribution plate 21, the distribution pipe 22 is connected with the lower end surface of the distribution plate 21 and extends downward from the distribution plate 21 , the distribution pipe 22 is a square pipe, and a plurality of distribution pipes 22 correspond to a plurality of blanking inlets 23 one by one. The lower end of the distribution pipe 22 is provided with a blanking outlet 24. Correspondingly, the lower end of the distribution pipe 22 extends into the upper end of the corresponding drop pipe 3, there is a gap between the top of the drop pipe 3 and the lower end surface of the distribution plate 21, and there is a gap between the distribution pipe 22 and the corresponding drop pipe 3. With a gap, the flue gas inlet 131 is located below the distribution plate 21 .

Specifically, as shown in FIG. 5 , the distribution plate 21 is provided with through holes having the same shape as the distribution pipe 22 , the through holes are arranged in parallel and equidistant, the cross section of the distribution pipe 22 is square, and the distribution pipe 22 extends along the vertical direction. It should be noted that the shapes of the blanking inlet 23 and the blanking outlet 24 are both square. As a result, the adsorbent can flow out from the distributor 2 evenly, avoiding dead angles in the flow, and improving the adsorption efficiency. The geometric center of the distribution pipe 22 in the horizontal direction coincides with the geometric center of the discharge pipe 3 in the horizontal direction. Thus, the adsorbent flowing out of the distribution pipe 222 can directly fall into the drop pipe 3, avoiding the accumulation of the adsorbent flowing from the distributor 2 into the drop pipe 3 and causing accumulation, and improving the flow of the adsorbent in the inner cavity. fluency.

In some embodiments, the vertical dimension of the gap between the top end of the drop tube 3 and the lower end surface of the distribution plate 21 is 20mm-100mm. Specifically, the above-mentioned size can be any value between 20mm and 100mm. For example, the vertical size of the gap between the top of the drop tube 3 and the lower end surface of the distribution plate 21 can be 33mm, 40mm, or 60.5mm. , 88m, etc.

Preferably, the vertical dimension of the gap between the top of the discharge pipe 3 and the lower end surface of the distribution plate 21 is 35 mm. This arrangement reduces the flow of smoke from between the distribution pipe 22 and the discharge pipe 3 on the one hand. The length of the passed path makes the flue gas flow more smoothly. On the other hand, it is convenient for the distribution pipe 22 to extend into the inside of the drop pipe 3, preventing the adsorbent particles from splashing out of the tower body 1 through the gap between the distribution pipe 22 and the drop pipe 3. , reducing the loss of adsorbent.

In some embodiments, the distance between the outer peripheral wall of the distribution pipe 22 and the corresponding inner peripheral wall of the discharge pipe 3 is 5mm-40mm in the horizontal direction. Specifically, the size can be any value between 50mm and 100mm. For example, the distance between the outer peripheral wall of the distribution pipe 22 and the inner peripheral wall of the corresponding drop pipe 3 in the horizontal direction can be 9mm, 15.5mm, 26mm, 40mm etc.

Preferably, the distance between the outer peripheral wall of the distribution pipe 22 and the inner peripheral wall of the corresponding downcomer 3 is 25mm in the horizontal direction, so that on the one hand, the distance between the flue gas passing between the distribution pipe 22 and the downcomer 3 is reduced. The length of the path makes the flue gas flow more smoothly. On the other hand, it is convenient for the distribution pipe 22 to extend into the inside of the drop pipe 3, preventing the adsorbent particles from splashing out of the tower body 1 through the gap between the distribution pipe 22 and the drop pipe 3, reducing the loss of adsorbent.

In some embodiments, the length of the part of the distribution pipe 22 protruding into the discharge pipe 3 is 5mm-40mm. Specifically, the length of the part of the distribution pipe 22 that extends into the blanking pipe 3 is the distance between the bottom end of the blanking outlet 24 and the upper end of the blanking pipe 3 in the vertical direction. The length of the part inside the pipe 3 can be any value between 5mm and 40mm. For example, the length of the part of the distribution pipe 22 protruding into the discharge pipe 3 can be 9mm, 15.5mm, 26mm, 40mm, etc.

Preferably, the length of the part of the distribution pipe 22 protruding into the discharge pipe 3 is 25 mm, which reduces the path length of the flue gas passing between the distribution pipe 22 and the discharge pipe 3 on the one hand, and makes the flow of the flue gas more stable. Smooth, on the other hand, the extension of the distribution pipe 22 into the drop pipe 3 can effectively prevent the adsorbent particles from splashing out of the tower body 1 through the gap between the distribution pipe 22 and the drop pipe 3, reducing the loss of the adsorbent.

In some embodiments, a plurality of blanking inlets 23 are arranged in multiple rows, each row of blanking inlets 23 includes several blanking inlets 23, and several blanking inlets 23 in each row of blanking inlets 23 are arranged at intervals along the first direction A plurality of rows of blanking inlets 23 are arranged at intervals in the second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of blanking inlets 23 are aligned in the second direction.

Specifically, the distribution plate 21 is rectangular, the length of the distribution plate 21 is 1000mm-3000mm, the width of the distribution plate 21 is 500mm-1500mm, the first direction is the length direction of the distribution plate 21, and the second direction is the width direction of the distribution plate 21 . It should be noted that, as shown in FIG. 4 , the first direction is the left-right direction, and the second direction is the front-rear direction.

Preferably, the length of the distribution plate 21 is 2000 mm, and the width of the distribution plate 21 is 1000 mm. Such an arrangement facilitates fixing the distribution plate 21 on the tower body 1 .

In some other embodiments, the distribution plate 21 may be circular, oval, triangular, etc.

In some embodiments, the edges of the blanking inlet 23 are square, and the side length of the blanking inlet 23 is 150mm-300mm. Specifically, the side length of the blanking inlet 23 can be any value between 150mm and 300mm, for example, the side length of the blanking inlet 23 can be 160mm, 199.5mm, 266mm, 299mm and so on.

Preferably, the side length of the blanking inlet 23 is 200 mm, so that more blanking inlets 23 can be arranged on the distribution plate 21 .

In some embodiments, the interval between two adjacent blanking inlets 23 in the first direction is 20mm-100mm, and the interval between two adjacent blanking inlets 23 in the second direction is 20mm-100mm. 100mm.

Specifically, the distance between two adjacent blanking inlets 23 is the distance between two nearest points of two adjacent blanking inlets 23 . It should be noted that the interval between two adjacent blanking inlets 23 in the first direction and the interval between two adjacent blanking inlets 23 in the second direction may be the same or different.

Preferably, the interval between two adjacent blanking inlets 23 in the first direction is 50mm, and the interval between two adjacent blanking inlets 23 in the second direction is 50mm. This arrangement can arrange more Many blanking inlets 23.

In some embodiments, the feeding tube 3 is a circular tube, and the feeding tube 3 includes a first section 31 and a second section 32, the diameter of the first section 31 is greater than the diameter of the second section 32, and the lower end of the first section 31 is in contact with the second section 32. The upper ends of the second section 32 are connected, and the lower end of the distribution pipe 22 extends into the first section 31 of the corresponding drop pipe 3 .

Specifically, the width of the first section 31 and the second section 32 is the size of the first section 31 and the second section 32 along the first direction, and the length of the first section 31 and the second section 32 is the dimension of the first section 31 and the second section 32. The size of the second section 32 along the second direction, the length of the second section 32 may be equal to that of the first section 31 , or the length of the second section 32 may be smaller than the length of the first section 31 . The width of the first segment 31 is greater than the width of the second segment 32 . As shown in Figure 6, the blanking tube 3 is a round tube for easy processing.

In some other embodiments, as shown in FIG. 7 , the drop tube 3 can also be a square tube.

In some embodiments, the drop tube 3 extends vertically, and the length of the drop tube 3 is 500mm-800mm. Specifically, the length of the drop tube 3 can be any value between 500mm and 800mm, for example, the length of the drop tube 3 can be 505mm, 620.7mm, 700mm, 786.85m, etc.

Preferably, the length of the drop tube 3 is 740mm, so that the material flows down smoothly

In some embodiments, the flue gas inlet 131 is located above the blanking outlet 24 .

Specifically, the height of the lowermost end of the flue gas inlet 131 is higher than the height of the blanking outlet 24 . Therefore, the flue gas inlet 131 is completely located above the blanking outlet 24, ensuring that when the adsorbent falls from the blanking pipe 3, it will not splash out of the tower body 1 through the flue gas inlet 131, thereby improving the efficiency of adsorbent collection.

In some embodiments, the cavity further includes a discharge section 14 located below the cloth section 11 , the discharge section 14 is in an inverted cone shape, and the discharge port 141 communicates with the bottom of the discharge section 14 .

Specifically, the cavity refers to the space inside the tower body 1, the discharge section 14 is an inverted quadrangular pyramid, the top of the discharge section 14 is connected with the inlet section 13, the discharge section 14 is a hollow structure, and the inside of the discharge section 14 The space is connected with the cavity, the cross-sectional area of the discharge section 14 gradually decreases along the direction from top to bottom, and the discharge port 141 is arranged at the lower end of the discharge section 14 . Thus, after the adsorbent completes the adsorption of harmful components in the flue gas, it falls into the discharge section 14 through the discharge pipe 3 and is collected in the discharge section 14. After a certain amount of adsorbent is collected, it is discharged from the discharge section 14 The material port 141 is discharged, and the recovered adsorbent is processed in the next step. When the material outlet 141 is closed, the harmful components escaping from the adsorbent flow upward together with the flue gas entering the flue gas inlet 131, and will not be volatilized. to the atmosphere.

In some embodiments, the height of the discharge section 14 is 1.0m-3.0m. Specifically, the height of the discharge section 14 is the vertical distance between the top of the discharge section 14 and the bottom of the discharge section 14 . The height of the discharge section 14 can be any value between 1.0m and 3.0m, for example, the height of the discharge section 14 can be 1.1m, 2.0m, 2.1m, 2.85m and so on.

Preferably, the height of the discharge section 14 is 1.8m, so that the material flows downward smoothly.

In some embodiments, the height of the moving bed adsorption tower is 4.0m-8.0m. Specifically, the height of the moving bed adsorption tower is the vertical distance between the feed port 111 and the discharge port 141 . The height of the moving bed adsorption tower can be any value between 4.0m and 8.0m, for example, the height of the moving bed adsorption tower can be 4.1m, 5.02m, 6.15m, 7.8m, etc.

Preferably, the height of the moving bed adsorption tower is 6.02m, and the setting in this way fully considers the height of the material layer and the space occupied.

In some embodiments, the height of the intake section 13 is 1.0m-2.0m, the height of the filler section 12 is 2.0m-3.0m, and the height of the cloth section 11 is 0.5m-1m.

Specifically, the height of the filler section 12 is greater than the sum of the inlet section 13 and the cloth section 11, for example, the height of the inlet section 13 is 1.5m, the height of the cloth section 11 is 0.6m, and the height of the filler section 12 is 2.5m. This, because the height of the packing section 12 is greater than the sum of the intake section 13 and the cloth section 11, the time that the adsorbent resides in the packing section 12 is greater than the sum of the residence time in the intake section 13 and the cloth section 11, increasing the The time for the adsorbent to adsorb the flue gas, thereby improving the adsorption efficiency.

Preferably, the height of the air inlet section 13 is 1.45m, the height of the packing section 12 is 2.05m, and the height of the cloth section 11 is 0.7m, so that the cloth can be covered with the cloth board 21 by such arrangement.

In some embodiments, the space velocity of the moving bed adsorption tower is 600h ^-1 -1500h ^-1 . Specifically, the space velocity refers to the ratio of the flue gas flow rate of the moving bed adsorption tower to the packing volume of the adsorbent in the moving bed adsorption tower. As a result, the space velocity of the moving bed adsorption tower is high, and the filling volume of the moving bed adsorption tower can be smaller than that of the existing moving bed adsorption tower under the same flue gas flow rate, so that the volume of the moving bed adsorption tower can be reduced , It can also reduce the loading amount of adsorbent in the tower.

Preferably, the space velocity of the moving bed adsorption tower is 1200h ^-1 -1500h ^-1 , so that the moving bed adsorption tower has an optimal adsorption effect.

The flue gas purification system according to the embodiment of the present invention includes: a flue gas cooling device, the flue gas cooling device has a smoke inlet and a smoke outlet, and the flue gas cooling device is used to cool the flue gas entering from the smoke inlet to room temperature and Below: moving bed adsorption tower, the moving bed adsorption tower is the moving bed adsorption tower according to any of the above-mentioned embodiments, the smoke outlet of the flue gas cooling device is communicated with the flue gas outlet 121 of the moving bed adsorption tower, and the moving bed adsorption tower is used for Adsorb the flue gas.

Optionally, the temperature of the flue gas entering the flue gas inlet 131 is -100° C. to room temperature (for example, the room temperature is 25° C.). Optionally, the adsorbent is activated coke (carbon).

The flue gas purification system provided in this example adopts the low-temperature adsorption method when adsorbing the flue gas, and utilizes the dissolution characteristics and adsorption characteristics of the pollutant components in the flue gas at low temperatures to remove pollutants, and can simultaneously realize desulfurization and denitrification . Among them, the sulfur dioxide in the flue gas is mainly physically adsorbed, the desorption temperature is low, the loss of the adsorbent is low, and the replenishment of the adsorbent is low, which reduces the operating cost. Moreover, the flue gas purification system that adsorbs at low temperature has a large adsorption capacity for pollutants, a small amount of adsorbent loading, and a small footprint for equipment such as moving bed adsorption towers.

It should be noted that when the flue gas purification system provided in this example performs adsorption and purification of the flue gas, the NO _x components that are difficult to remove in the flue gas are oxidized to _NO by adsorption and removal at a low temperature through the mechanism of oxidation adsorption. It needs to inject _NH3 for catalytic reduction, and the operation cost is low. The flue gas purification system provided in this embodiment can absorb more than 99% of _NOx in the flue gas, and the denitrification efficiency is obviously better than the 70-80% denitrification efficiency in the prior art.

In describing the present invention, it should be understood that the terms "center", "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", " Back", "Left", "Right", "Vertical", "Horizontal", "Top", "Bottom", "Inner", "Outer", "Clockwise", "Counterclockwise", "Axial", The orientation or positional relationship indicated by "radial", "circumferential", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying the referred device or element Must be in a particular orientation, be constructed in a particular orientation, and operate in a particular orientation, and therefore should not be construed as limiting the invention.

In addition, the terms "first" and "second" are used for descriptive purposes only, and cannot be interpreted as indicating or implying relative importance or implicitly specifying the quantity of indicated technical features. Thus, the features defined as "first" and "second" may explicitly or implicitly include at least one of these features. In the description of the present invention, "plurality" means at least two, such as two, three, etc., unless otherwise specifically defined.

In the present invention, unless otherwise clearly specified and limited, terms such as "installation", "connection", "connection" and "fixation" should be understood in a broad sense, for example, it can be a fixed connection or a detachable connection , or integrated; can be mechanically connected, can also be electrically connected or can communicate with each other; can be directly connected, can also be indirectly connected through an intermediary, can be the internal communication of two components or the interaction relationship between two components, Unless expressly defined otherwise. Those of ordinary skill in the art can understand the specific meanings of the above terms in the present invention according to specific situations.

In the present invention, unless otherwise clearly specified and limited, the first feature may be in direct contact with the first feature or the first and second feature may be in direct contact with the second feature through an intermediary. touch. Moreover, "above", "above" and "above" the first feature on the second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. "Below", "beneath" and "beneath" the first feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is less horizontally than the second feature.

As used herein, the terms "one embodiment," "some embodiments," "example," "specific examples," or "some examples" mean specific features, structures, materials, or features described in connection with the embodiment or example. A feature is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the described specific features, structures, materials or characteristics may be combined in any suitable manner in any one or more embodiments or examples. In addition, those skilled in the art can combine and combine different embodiments or examples and features of different embodiments or examples described in this specification without conflicting with each other.

Although the embodiments of the present invention have been shown and described above, it can be understood that the above embodiments are exemplary and should not be construed as limiting the present invention, those skilled in the art can make the above-mentioned The embodiments are subject to changes, modifications, substitutions and variations.

Claims (8)

1. A moving bed adsorption tower, characterized in that, comprising: A tower body, the tower body has a cavity, the tower body is provided with a feeding port, a material outlet, a flue gas inlet and a flue gas outlet communicating with the cavity, and the cavity is in the flow direction of the flue gas It has an air inlet section, a packing section and a cloth section, and the packing section is used for filling the adsorbent; A distributor, the distributor is arranged in the tower body, the distributor includes a plurality of blanking inlets and a plurality of blanking outlets corresponding to the blanking inlets, and the distributor is located below the packing section so that the adsorbent in the packing section flows out through the blanking inlet and the corresponding blanking outlet, wherein the blanking inlet is square; A plurality of drop tubes, a plurality of the drop tubes correspond to a plurality of the drop outlets, the drop outlets are located in the drop tube, and there is a gap between the drop tube and the distributor The gap is for smoke to pass through, the smoke inlet is located below the blanking inlet, and the blanking pipe is located above the discharge port; The distributor includes a distribution plate and a plurality of distribution pipes, the blanking inlet is arranged on the distribution plate, the distribution pipe is connected with the lower end surface of the distribution plate and extends downward from the distribution plate, the The distribution pipe is a square pipe, and a plurality of the distribution pipes correspond to a plurality of the blanking inlets one by one. The distribution pipes are in one-to-one correspondence, the lower end of the distribution pipe extends into the upper end of the corresponding drop pipe, there is a gap between the top end of the drop pipe and the lower end surface of the distribution plate, and the distribution pipe There is a space between the tube and the corresponding drop tube, and the flue gas inlet is located below the distribution plate; The feeding tube is a round tube, and the dropping tube includes a first section and a second section, the diameter of the first section is larger than the diameter of the second section, and the lower end of the first section is connected to the second section. The upper ends of the two sections are connected, and the lower end of the distribution pipe extends into the corresponding first section of the discharge pipe. 2 . The moving bed adsorption tower according to claim 1 , wherein the vertical dimension of the gap between the top of the downcomer and the lower end surface of the distribution plate is 20mm-100mm. 3. The moving bed adsorption tower according to claim 1, characterized in that the distance between the outer peripheral wall of the distribution pipe and the corresponding inner peripheral wall of the downcomer is 5mm-40mm in the horizontal direction. 4. The moving bed adsorption tower according to any one of claims 1-3, characterized in that, the length of the part of the distribution pipe protruding into the drop pipe is 5mm-40mm. 5. The moving bed adsorption tower according to any one of claims 1-3, characterized in that, a plurality of said blanking inlets are arranged in multiple rows, and each row of blanking inlets includes several said blanking inlets, each A number of blanking inlets in the row of blanking inlets are arranged at intervals along the first direction, and multiple rows of blanking inlets are arranged at intervals in the second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows The blank inlets are aligned in the second direction. 6. The moving bed adsorption tower according to claim 5, characterized in that, the edge of the blanking inlet is square, and the side length of the blanking inlet is 150mm-300mm. 7. The moving bed adsorption tower according to claim 5, characterized in that, the interval between two adjacent blanking inlets in the first direction is 20mm-100mm, and in the second direction, the interval is 20mm-100mm. The interval between two adjacent blanking inlets is 20mm-100mm. 8. A flue gas purification system, characterized in that it comprises: A flue gas cooling device, the flue gas cooling device has a smoke inlet and a smoke outlet, and the flue gas cooling device is used to cool the flue gas entering from the smoke inlet to room temperature or below; A moving bed adsorption tower, the moving bed adsorption tower is the moving bed adsorption tower according to any one of claims 1-7, the flue gas outlet of the flue gas cooling device is connected to the moving bed adsorption tower of the moving bed adsorption tower The flue gas outlet is connected, and the moving bed adsorption tower is used to adsorb the flue gas.

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