CN113828108B - Flue gas purification system and moving bed adsorption tower - Google Patents
Flue gas purification system and moving bed adsorption tower Download PDFInfo
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- CN113828108B CN113828108B CN202111081479.2A CN202111081479A CN113828108B CN 113828108 B CN113828108 B CN 113828108B CN 202111081479 A CN202111081479 A CN 202111081479A CN 113828108 B CN113828108 B CN 113828108B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
- B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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Abstract
The invention discloses a flue gas purification system and a moving bed adsorption tower, wherein the moving bed adsorption tower comprises a tower body, a 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 circulation direction of flue gas; the distributor is arranged in the tower body and provided with a plurality of blanking ports, the distributor is positioned below the filler section, and the blanking ports are square; the plurality of blanking pipes correspond to the plurality of blanking ports one to one, the blanking pipes are located below the blanking ports and spaced from the blanking ports, the flue gas inlet is located below the blanking ports, and the blanking pipes are located above the discharge ports. The invention has the advantages of uniform adsorption and good adsorption effect.
Description
Technical Field
The application relates to the technical field of flue gas treatment, in particular to a flue gas purification system and a moving bed adsorption tower.
Background
The generation of a large amount of pollutants from coal-fired flue gas is one of the important factors endangering the atmospheric environment and human health. The fixed bed adsorption tower is usually adopted in the flue gas purification field to adsorb the purpose in order to realize purifying flue gas in the pollutant in the flue gas, but the fixed bed adsorption tower among the correlation technique ubiquitous filler layer pressure and density when using problem that absorption is inhomogeneous, adsorption effect is poor, adsorption efficiency reduces along with the live time extension, need stop work when needing to change the adsorbent in addition, seriously influences adsorption efficiency, has improved the operation degree of difficulty. In the related technology, the moving bed adsorption tower is adopted to enable the adsorbent to flow in the tower, so that the problem that the adsorption capacity of the fixed bed adsorption tower is reduced along with the prolonging of the service time is solved, but the problems of uneven smoke distribution and unsatisfactory purification effect still exist in the moving bed adsorption tower.
Disclosure of Invention
The present invention is directed to solving, at least in part, one of the technical problems in the related art. Therefore, the embodiment of the invention provides a moving bed adsorption tower which has the advantages of uniform adsorption and good adsorption effect.
The embodiment of the invention also provides a flue gas purification system comprising the moving bed adsorption tower.
The moving bed adsorption tower comprises a tower body, wherein a cavity is formed 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, the cavity is provided with an air inlet section, a filling section and a material distribution section in the circulation direction of flue gas, and the filling section is used for filling an adsorbent; the distributor is arranged in the tower body and provided with a plurality of blanking ports, and the distributor is positioned below the filling section so that the adsorbent in the filling section can flow out through the blanking ports, wherein the blanking ports are square; the blanking device comprises a plurality of blanking pipes, wherein the blanking pipes correspond to the blanking ports one to one, the blanking pipes are located below the blanking ports and have intervals between the blanking ports so that smoke can flow conveniently, the smoke inlet is located below the blanking ports, and the blanking pipes are located above the discharge ports.
The moving bed adsorption tower disclosed by the embodiment of the invention has the advantages of uniform adsorption and good adsorption effect.
In some embodiments, the distributor comprises a distribution plate, the blanking port is arranged on the distribution plate, the distribution plate is connected with the peripheral wall of the cavity, and the flue gas inlet is positioned below the distribution plate.
In some embodiments, a gap between a top end of the down pipe and a lower end surface of the distribution plate is 20mm to 100mm in a vertical direction.
In some embodiments, the plurality of blanking openings are arranged in multiple rows, each row of blanking openings includes a plurality of blanking openings, the plurality of blanking openings in each row of blanking openings are arranged at intervals along a first direction, the plurality of rows of blanking openings are arranged at intervals in a second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of blanking openings are aligned in the second direction.
In some embodiments, the edge of the blanking opening is square, and the side of the blanking opening is 150mm-300mm.
In some embodiments, the interval between two adjacent blanking openings in the first direction is 20mm to 100mm, and the interval between two adjacent blanking openings in the second direction is 20mm to 100mm.
In some embodiments, the blanking pipe is a circular pipe, the blanking pipe extends in a vertical direction, and the diameter of the blanking pipe is 100mm-400mm.
In some embodiments, the blanking pipe is a round pipe, the blanking pipe comprises a first section and a second section, the diameter of the first section is larger than that of the second section, and the lower end of the first section is connected with the upper end of the second section.
In some embodiments, the diameter of the first section is greater than or equal to the radius of the packing angle of the adsorbent.
The flue gas purification system comprises a flue gas cooling device, wherein the flue gas cooling device is provided with a flue gas inlet and a flue gas outlet and is used for cooling the flue gas entering from the flue gas inlet to room temperature or below; the flue gas cooling device comprises a flue gas outlet, a moving bed adsorption tower and a flue gas cooling device, wherein the flue gas outlet is communicated with the flue gas outlet of the moving bed adsorption tower, and the moving bed adsorption tower is used for adsorbing the flue gas.
Drawings
Fig. 1 is a front view of a moving bed adsorption column according to an embodiment of the present invention.
Fig. 2 is a top view of a moving bed adsorption column according to an embodiment of the present invention.
Fig. 3 isbase:Sub>A cross-sectional view atbase:Sub>A-base:Sub>A in fig. 2.
Fig. 4 is a 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 the plurality of down tubes of FIG. 3
Reference numerals are as follows:
a tower body 1; a material distribution section 11; a feed port 111; a filler section 12; a flue gas outlet 121; an air intake section 13; a flue gas inlet 131; a discharge section 14; a discharge port 141;
a distributor 2; a distribution plate 21; a blanking port 22;
a blanking pipe 3; a first section 31; second segment 32:
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
As shown in fig. 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 down pipes 3.
The tower body 1 is internally provided with a cavity, the tower body 1 is provided with a feed inlet 111, a discharge outlet 141, a flue gas inlet 131 and a flue gas outlet 121 which are communicated with the cavity, the cavity is provided with an air inlet section 13, a filler section 12 and a material distribution section 11 in the circulation direction of flue gas, and the filler section 12 is used for filling an adsorbent;
specifically, the flue gas inlet 131 is communicated with the gas inlet section 13, the flue gas outlet 121 is communicated with the material distribution section 11, the charging opening 111 and the flue gas outlet 121 are located above the filling section 12, and the discharge opening 141 and the flue gas inlet 131 are located below the filling section 12. It should be noted that the flue gas flowing direction is from the flue gas inlet 131 to the flue gas outlet 121, and the distributing section 11, the filling section 12 and the air inlet section 13 are sequentially arranged along the direction from top to bottom. From this, the flue gas gets into tower body 1's inside and flows from tower body 1's upside from tower body 1's lower half of tower body 1, the adsorbent gets into tower body 1 and flows from tower body 1's lower extreme from tower body 1's upside, the flow direction of flue gas is opposite with the flow direction of adsorbent, the concentration of nitrogen and sulphur reduces along with the flue gas rises gradually in the flue gas, the adsorption effect of adsorbent reduces along with the time with the flue gas contact gradually, the adsorbent contact of the better adsorption effect of flue gas of lower nitrogen and sulphur concentration, can effectively reduce the concentration of nitrogen and sulphur in following gas outlet 121 exhaust gas, and the adsorption efficiency is improved.
The distributor 2 is arranged in the tower body 1, the distributor 2 is provided with a plurality of blanking ports 22, the distributor 2 is positioned below the packing section 12 so that the adsorbent in the packing section 12 can flow out through the blanking ports 22, and the blanking ports 22 are square;
specifically, as shown in fig. 4, the blanking port 22 is square, so that the space utilization rate of the blanking port 22 in the horizontal direction is improved, and the blanking efficiency is improved. The blanking ports 22 are through holes on the distributor 2, and the blanking ports 22 are arranged in parallel at intervals and are equal in distance. From this, the adsorbent passes in blanking mouth 22 gets into blanking pipe 3, and the adsorbent is roughly the same through each blanking mouth 22's of evenly arranging flow, has delayed the downward speed that flows of adsorbent on the one hand, has increased the time of adsorbent granule and flue gas contact, and on the other hand avoids the adsorbent to concentrate from the position outflow that is closer to tower body 1 center, produces the dead angle in the flow, has improved the efficiency that the adsorbent flows to adsorption effect has been improved.
The plurality of blanking pipes 3 correspond to the plurality of blanking ports 22 one by one, the blanking pipes 3 are located below the blanking ports 22 and have intervals with the blanking ports 22 so that smoke can flow, the smoke inlet 131 is located below the blanking ports 22, and the blanking pipes 3 are located above the discharge ports 141.
Specifically, the geometric center of the blanking port 22 in the horizontal direction is the same as the geometric center of the blanking pipe 3 in the horizontal direction, the upper end of the blanking pipe 3 is spaced from the lower end of the distributor 2, and the upper edge of the flue gas inlet 131 is located below the blanking port 22 to ensure that the flue gas inlet 131 is completely located below the blanking port 22. From this, the flue gas gets into tower body 1 back from flue gas inlet 131, and in the interval entering filler section 12 between blanking pipe 3 and blanking mouth 22, the path that gets into the seasoning section at the flue gas is shorter more smooth-going, and the pressure drop that causes because energy loss when the flue gas flows is low, has improved the smooth degree that the flue gas flows at filler section 12 to adsorption effect has been improved.
In some embodiments, the distributor 2 comprises a distribution plate 21, the blanking opening 22 is disposed on the distribution plate 21, the distribution plate 21 is connected to the peripheral wall of the cavity, and the flue gas inlet 131 is located below the distribution plate 21.
Specifically, as shown in fig. 5, the distribution plate 21 is a porous flat plate, the blanking port 22 is a through hole on the distribution plate 21, the distribution plate 21 is horizontally arranged, and the lower end of the distribution plate 21 is higher than the upper end of the flue gas inlet 131. From this, distribution plate 21 horizontal arrangement can guarantee that the adsorbent distributes uniformly in distribution plate 21's top, thereby guarantees that the blanking is even to improve the efficiency of blanking, and the lower extreme of distribution plate 21 is higher than the upper end of flue gas inlet 131 and can makes whole flue gas all pass from blanking mouth 22, has improved the contact time of flue gas and adsorbent granule to absorbent efficiency has been improved.
In some embodiments, the gap between the top end of the drop tube 3 and the lower end surface of the distribution plate 21 has a dimension in the vertical direction of 20mm to 100mm.
Specifically, the size of the gap between the down pipe 3 and the distribution plate 21 in the vertical direction may be any value between 20mm and 100mm. Preferably, the gap between the down pipe 3 and the distribution plate 21 has a dimension of 75mm in the vertical direction, which is advantageous for increasing the flow rate of the flue gas passing through the gap between the down pipe 3 and the distribution plate 21.
In some embodiments, the plurality of blanking openings 22 are arranged in multiple rows, each row of blanking openings 22 includes a plurality of blanking openings 22, the plurality of blanking openings 22 in each row of blanking openings 22 are arranged at intervals along a first direction, the plurality of rows of blanking openings 22 are arranged at intervals along a second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of blanking openings 22 are aligned along the second direction.
Specifically, the distances between two adjacent rows of the blanking openings 22 are equal, and the distances between adjacent blanking openings 22 in each row of the blanking openings 22 are the same, and it should be noted that the distance between two adjacent blanking openings 22 in the first direction may be the same as or different from the distance between two adjacent blanking openings 22 in the second direction. As shown in fig. 4, the first direction is a left-right direction, and the second direction is a front-back direction.
In some embodiments, the distribution plate 21 is rectangular, the length of the distribution plate 21 is 1000mm to 3000mm, the width of the distribution plate 21 is 500mm to 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. Preferably, the length of the distribution plate 21 is 2000mm, and the width of the distribution plate 21 is 1000mm, so that the distribution plate 21 can be provided with more material discharge ports 22.
In some embodiments, the edge of the drop opening 22 is square, and the edge of the drop opening 22 is 150mm to 300mm.
Specifically, the side length of the blanking opening 22 may be any value between 150mm and 300mm, for example, the side length of the blanking opening 22 may be 160mm, 199.5mm, 266mm, 299mm, and the like. Preferably, the side of the blanking opening 22 is 200mm, so that more blanking openings 222 can be arranged on the distribution plate 21.
In some embodiments, the spacing between two blanking ports 22 adjacent in the first direction is 20mm to 100mm, and the spacing between two blanking ports 22 adjacent in the second direction is 20mm to 100mm.
Specifically, the distance between two adjacent blanking ports 22 is the distance between the two closest points of the two adjacent blanking ports 22. It should be noted that the interval between two adjacent blanking ports 22 in the first direction may be the same as or different from the interval between two adjacent blanking ports 22 in the second direction.
In some embodiments the down pipe 3 is a round pipe, the down pipe 3 extending in a vertical direction, the down pipe 3 having a diameter of 100-400 mm.
In particular, the diameter of the down pipe 3 refers to the inner diameter of the down pipe 3, and the diameter of the down pipe 3 may be any value from 100mm to 400mm. The down pipe 3 may be of the same diameter everywhere or of different diameters at different locations.
In other embodiments, the down pipe 3 may also be a square pipe.
In some embodiments the down pipe 3 is a round pipe, the down pipe 3 comprising a first section 31 and a second section 32, the first section 31 having a larger diameter than the second section 32, the lower end of the first section 31 being connected to the upper end of the second section 32.
Specifically, as shown in fig. 6, the first section 31 and the second section 32 are connected by a connecting plate, the connecting plate is concentric and circular, the outer diameter of the connecting plate is the same as the diameter of the first section 31, the inner diameter of the connecting plate is the same as the diameter of the second section 32, and the connecting plate is horizontally arranged. From this, adsorbent granule can pile up earlier and fall into ejection of compact section 14 through second section 32 in first section 31, can prevent that the flue gas from producing the leakage of flue gas in the blanking pipe 3 entering ejection of compact section 14. In addition, the blanking pipe 3 is a round pipe, so that the processing is convenient.
In some embodiments, the diameter of the first section 31 is greater than or equal to the radius of the angle of repose of the adsorbent.
Specifically, the adsorbent particles will fall down to the joint of the first section 31 and the second section 32, and pile up in the first section 31 of the down pipe 3 to form a structure similar to a cone, the radius of the pile-up angle refers to the radius of the cone, and the width of the upper end opening of the down pipe 3 is the distance between the two ends of the down pipe 3 in the first direction. From this, two walls about the blanking pipe 3 can not influence the piling up of adsorbent, have reduced the influence that blanking pipe 3 appearance passes 3 flows of blanking pipe to the adsorbent granule to avoid the adsorbent granule to spill between blanking pipe 3.
In some embodiments the down pipe 3 extends in a vertical direction, the length of the down pipe 3 being 500-800 mm. In particular, the length of the down pipe 3 may be any value between 500mm and 800mm, for example, the length of the down pipe 3 may be 505mm, 620.7mm, 700mm, 786.85m, etc.
Preferably, the down pipe 3 has a length of 740mm, so that the adsorbent particles smoothly flow downward.
In some embodiments, the flue gas inlet 131 is located below the blanking opening 22.
Specifically, the height of the uppermost end of the flue gas inlet 131 is lower than the height of the blanking port 22. Therefore, the flue gas inlet 131 is completely located below the blanking port 22, so that after the flue gas enters the tower body 1, all the flue gas enters the filler section through the blanking port 22, the contact time of the flue gas and the adsorbent is prolonged, and the adsorption efficiency is improved.
In some embodiments, the cavity further comprises a discharge section 14 located below the material distribution section 11, the discharge section 14 is in an inverted cone shape, and the discharge port 141 is communicated with the bottom of the discharge section 14.
Specifically, the cavity is the inside space of tower body 1, goes out the material section 14 and is the four pyramid shape of falling, and the top and the section of admitting air 13 of going out material section 14 are connected, and it is hollow structure to go out material section 14, and the inside space of the material section 14 links to each other with the cavity, and the sectional area of the material section 14 of going out reduces along the direction from the top to the bottom gradually, and discharge gate 141 sets up the lower extreme at the material section 14 of going out. From this, the adsorbent falls into ejection of compact section 14 through blanking pipe 3 after accomplishing the absorption to harmful component in the flue gas to collect in ejection of compact section 14, after collecting a certain amount of adsorbent, discharge from discharge gate 141, carry out processing on next step to the adsorbent of retrieving, when discharge gate 141 seals, harmful component that escapes in the adsorbent and the flue gas that gets into in the gas inlet 131 upwards flow together, can not volatilize in the atmosphere.
In some embodiments, the discharge section 14 has a height of 1.0m to 3.0m. Specifically, the height of the discharging section 14 is the distance between the top of the discharging section 14 and the bottom of the discharging section 14 in the vertical direction. The height of the discharge section 14 may be any value between 1.0m and 3.0m, for example, the height of the discharge section 14 may be 1.1m, 2.0m, 2.1m, 2.85m, etc. Preferably, the height of the discharge section 14 is 1.8m, so that the material flows smoothly downwards.
In some embodiments, the moving bed adsorption column has a height of 4.0m to 8.0m. Specifically, the height of the moving bed adsorption tower is the distance between the feed port 111 and the discharge port 141 in the vertical direction. The height of the moving bed adsorption column may be any value between 4.0m and 8.0m, for example, the height of the moving bed adsorption column may be 4.1m, 5.02m, 6.15m, 7.8m, etc. Preferably, the height of the adsorption tower of the moving bed is 6.02m, and the arrangement fully considers the height of a material layer and the occupied space.
In some embodiments, the height of the air inlet section 13 is 1.0m to 2.0m, the height of the filling section 12 is 2.0m to 3.0m, and the height of the cloth section 11 is 0.5m to 1m.
Specifically, the height of the packing section 12 is greater than the sum of the air inlet section 13 and the material distribution section 11, for example, the height of the air inlet section 13 is 1.5m, the height of the material distribution section 11 is 0.6m, and the height of the packing section 12 is 2.5m, so that the time for the adsorbent to adsorb the flue gas is increased because the height of the packing section 12 is greater than the sum of the air inlet section 13 and the material distribution section 11, and the time for the adsorbent to remain in the packing section 12 is greater than the sum of the time for the adsorbent to remain in the air inlet section 13 and the material distribution section 11, thereby improving the adsorption efficiency.
Preferably, the height of the air inlet section 13 is 1.45m, the height of the filling section 12 is 2.05m, and the height of the distributing section 11 is 0.7m, so that the distributing plate 21 can be fully distributed.
In some embodiments, the space velocity of the moving bed adsorption column 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. Therefore, the airspeed of the moving bed adsorption tower is higher, 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, the volume of the moving bed adsorption tower can be reduced, and the filling amount of the adsorbent in the tower can also be reduced.
Preferably, the space velocity of the adsorption tower of the moving bed is 1000h -1 -1500h -1 The adsorption effect of the adsorption tower in the moving bed is optimized.
The flue gas purification system comprises a flue gas cooling device, wherein the flue gas cooling device is provided with a flue gas inlet and a flue gas outlet, and is used for cooling the flue gas entering from the flue gas inlet to room temperature or below; the flue gas cooling device comprises a flue gas outlet 121, a moving bed adsorption tower, a flue gas cooling device and a flue gas cooling device.
Optionally, the temperature of the flue gas entering the flue gas inlet 131 is between-100 ℃ and room temperature (e.g., room temperature is 25 ℃). Optionally, the adsorbent is activated coke (carbon).
The flue gas purification system that this embodiment provided adopts the low temperature adsorption's mode when adsorbing the flue gas, utilizes the dissolution characteristic and the adsorption characteristic of pollutant component at low temperature in the flue gas to carry out deviating from of pollutant, can realize SOx/NOx control simultaneously. The sulfur dioxide in the flue gas is mainly subjected to physical adsorption, the desorption temperature is low, the loss of the adsorbent is low, the supplement amount of the adsorbent is low, and the operation cost is reduced. In addition, the flue gas purification system for adsorbing at low temperature has large pollutant adsorption capacity, small adsorbent filling amount and small occupied area of equipment such as a moving bed adsorption tower and the like.
It should be noted that, when the flue gas purification system provided by this embodiment performs adsorption purification on flue gas, NO that is difficult to be removed from flue gas x The component is oxidized into NO by using a low-temperature oxidation adsorption mechanism 2 Adsorption and removal without spraying NH 3 The catalytic reduction is carried out, and the operation cost is low. The flue gas purification system provided by the embodiment can be used for purifying NO in flue gas x The adsorption ratio of the denitration catalyst is more than 99 percent, and the denitration efficiency is obviously superior to 70-80 percent of denitration efficiency in the prior art.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, but are not intended to indicate or imply that the device or element so referred to must have a particular orientation, be constructed in a particular orientation, and be operated in a particular manner, and are not to be construed as limiting the invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or to implicitly indicate the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of the feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be interconnected within two elements or in a relationship where two elements interact with each other unless otherwise specifically limited. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the present disclosure, the terms "one embodiment," "some embodiments," "example," "specific example," or "some examples" and the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Moreover, various embodiments or examples and features of various embodiments or examples described in this specification can be combined and combined by one skilled in the art without being mutually inconsistent.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (7)
1. A moving bed adsorption column, comprising:
the tower body is provided with a cavity, 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, the cavity is provided with an air inlet section, a filling section and a material distribution section in the circulation direction of flue gas, and the filling section is used for filling an adsorbent;
the distributor is arranged in the tower body and provided with a plurality of blanking ports, and the distributor is positioned below the filling section so that the adsorbent in the filling section can flow out through the blanking ports, wherein the blanking ports are square;
the blanking pipes correspond to the blanking ports one by one, are positioned below the blanking ports and are spaced from the blanking ports so that smoke can flow conveniently, the smoke inlet is positioned below the blanking ports, and the blanking pipes are positioned above the discharge ports;
the distributor comprises a distribution plate, the blanking port is arranged on the distribution plate, the distribution plate is connected with the peripheral wall of the cavity, and the flue gas inlet is positioned below the distribution plate;
the blanking pipe is a circular pipe and comprises a first section and a second section, the diameter of the first section is larger than that of the second section, and the lower end of the first section is connected with the upper end of the second section;
the size of a gap between the top end of the blanking pipe and the lower end face of the distribution plate in the vertical direction is 20-100 mm.
2. A moving bed adsorption tower according to claim 1, wherein the plurality of blanking ports are arranged in a plurality of rows, each row of blanking ports comprises a plurality of blanking ports, the plurality of blanking ports in each row of blanking ports are arranged at intervals along a first direction, the plurality of rows of blanking ports are arranged at intervals along a second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of blanking ports are aligned along the second direction.
3. The moving bed adsorption tower according to claim 2, wherein the edge of the blanking port is square, and the side length of the blanking port is 150mm to 300mm.
4. The moving bed adsorption column according to claim 2, wherein the interval between two blanking ports adjacent in the first direction is 20mm to 100mm, and the interval between two blanking ports adjacent in the second direction is 20mm to 100mm.
5. A moving bed adsorption tower according to claim 1, wherein the drop tube is a circular tube, the drop tube extending in a vertical direction, the drop tube having a diameter of 100mm to 400mm.
6. The moving bed adsorption column according to claim 1, wherein the diameter of the first section is equal to or greater than the radius of the angle of repose of the adsorbent.
7. A flue gas purification system, comprising:
the flue gas cooling device is provided with a flue gas inlet and a flue gas outlet and is used for cooling the flue gas entering from the flue gas inlet to room temperature or below;
the moving bed adsorption tower is according to any one of claims 1-6, a smoke outlet of the smoke cooling device is communicated with the smoke outlet of the moving bed adsorption tower, and the moving bed adsorption tower is used for adsorbing the smoke.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2021110285214 | 2021-09-02 | ||
| CN202111028521 | 2021-09-02 |
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| Publication Number | Publication Date |
|---|---|
| CN113828108A CN113828108A (en) | 2021-12-24 |
| CN113828108B true CN113828108B (en) | 2023-03-10 |
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| CN202111081479.2A Active CN113828108B (en) | 2021-09-02 | 2021-09-15 | Flue gas purification system and moving bed adsorption tower |
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| DE3611953A1 (en) * | 1985-11-09 | 1987-08-13 | Kraftwerk Union Ag | Device for the controlled withdrawal of free-flowing bulk material at the underside of a bulk material column, in particular of a moving-bed filter |
| DE3916325A1 (en) * | 1989-05-19 | 1990-11-22 | Grochowski Horst | WALKING BED REACTOR |
| DE4129167C1 (en) * | 1991-09-03 | 1992-12-10 | Nymic Anstalt, Schaan, Li |
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