CN113828111B - Moving bed adsorption tower with distributor and flue gas purification system - Google Patents
Moving bed adsorption tower with distributor and flue gas purification system Download PDFInfo
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- CN113828111B CN113828111B CN202111082809.XA CN202111082809A CN113828111B CN 113828111 B CN113828111 B CN 113828111B CN 202111082809 A CN202111082809 A CN 202111082809A CN 113828111 B CN113828111 B CN 113828111B
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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 moving bed adsorption tower with a distributor and a flue gas purification system. The tower body is internally provided with a cavity, the tower body is provided with a feeding port, a discharging port, a smoke inlet and a smoke outlet which are communicated with the cavity, the cavity is provided with an air inlet section, a filling section and an air outlet section in the circulation direction of smoke, 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 filler section so that the adsorbent in the filler section can flow out through the blanking ports; 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 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 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 moving bed adsorption tower with a distributor and a flue gas purification system.
Background
The generation of a large amount of pollutants from coal-fired flue gas is one of the important factors harming 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 non-uniform distribution of flue gas and non-ideal purification effect still exist in the moving bed adsorption tower.
Disclosure of Invention
The present invention is directed to solving, at least to some extent, 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 a gas inlet section, a filler section and a gas outlet section in the flowing direction of flue gas, and the filler 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 filler section so that the adsorbent in the filler section can flow out through the blanking ports; 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 provided 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, the gap between the top end of the down pipe and the lower end face of the distribution plate has a dimension in the vertical direction of 20mm to 100mm.
In some embodiments, the blanking ports are strip-shaped ports, the plurality of blanking ports are arranged at intervals in a first direction, the blanking ports extend in a second direction, and the first direction is perpendicular to the second direction.
In some embodiments, the blanking opening has a width of 80mm to 200mm, the distributor has a dimension L in the second direction, and the blanking opening has a length of 0.8L to 0.95L.
In some embodiments, the distance between two adjacent blanking ports is 100mm-300mm.
In some embodiments, the distribution plate is rectangular, the length of the distribution plate is 1000mm to 3000mm, the width of the distribution plate is 500mm to 1500mm, the first direction is the length direction of the distribution plate, and the second direction is the width direction of the distribution plate.
In some embodiments, the blanking pipe extends along a vertical direction, and the length of the blanking pipe in the vertical direction is 500mm-700mm.
In some embodiments, the width of the upper end opening of the down pipe is greater than or equal to the radius of the stacking angle of the adsorbent.
In some embodiments, the down pipe comprises a first section and a second section, the first section having a width greater than a width of the second section, a lower end of the first section being connected to an upper end of the second section.
In some embodiments, the first section has a width of 200mm to 400mm and the second section has a width of 100mm to 200mm.
In some embodiments, the flue gas inlet is located above the bottom end of the down pipe.
According to the embodiment of the invention, the flue gas purification system comprises:
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 flue gas outlet and a moving bed adsorption tower, 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.
Reference numerals are as follows:
a tower body 1; an air outlet 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; a second section 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 accompanying drawings are illustrative and intended to explain the present invention and should not be construed as limiting the present 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 a gas inlet section 13, a filler section 12 and a gas outlet 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 gas outlet section 11, the charging opening 111 and the flue gas outlet 121 are located above the filler section 12, and the discharge opening 141 and the flue gas inlet 131 are located below the filler section 12. It should be noted that the smoke flowing direction is from the smoke inlet 131 to the smoke outlet 121, and the air outlet section 11, the filler 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, and 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;
specifically, the blanking ports 22 are through holes on the distributor 2, and the blanking ports 22 are arranged in parallel at intervals and at equal intervals. 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, after the flue gas got into tower body 1 from flue gas inlet 131, in interval entering filler section 12 between blanking pipe 3 and blanking mouth 22, the route that gets into the condiment section at the flue gas was shorter smoother, and the pressure drop that arouses because energy loss when the flue gas flows is low, has improved the smooth degree that the flue gas flowed 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, 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 is 75mm in vertical dimension, and is set such that the flow rate of air passing through the gap is required to achieve the space velocity of the adsorption tower.
In some embodiments, the blanking opening 22 is a strip-shaped opening, the plurality of blanking openings 22 are arranged at intervals in a first direction, the blanking openings 22 extend in a second direction, and the first direction and the second direction are perpendicular to each other.
Specifically, as shown in fig. 4, the first direction is the left-right direction, the second direction is the front-back direction, and the blanking ports 22 are arranged at equal intervals along the first direction, so that the blanking ports 22 are strip-shaped, and not only can adsorbent particles fall into the blanking pipe 3 completely, but also can ensure a larger sectional area of the blanking ports 22, thereby ensuring the flowability of the adsorbent particles.
In other embodiments, the drop opening 22 may be circular, triangular, diamond-shaped, etc.
In some embodiments, the width of the drop opening 22 is 80mm to 200mm, the dimension of the distributor 2 in the second direction is L, and the length of the drop opening 22 is 0.8L to 0.95L.
Specifically, the width of the blanking opening 22 may be any value between 80mm and 200mm, for example, the width of the blanking opening 22 may be 85mm, 100mm, 151.8mm, 200mm, etc. Preferably, the blanking opening 22 has a width of 290mm, which is set to allow the flow rate of the adsorbent particles through the blanking opening 22 to meet the design requirements.
It should be noted that the width of the blanking opening 22 is the size of the blanking opening 22 in the first direction, and the length of the blanking opening 22 is the size of the blanking opening 22 in the second direction.
Preferably, the dimension of the distributor 2 in the second direction is 1850mm and the length of the blanking port 22 is 900mm, which is set such that the flow rate of the adsorbent particles through the blanking port 22 is as designed.
In some embodiments, the distance between two adjacent blanking openings 22 is 100mm-300mm.
Specifically, the interval between two adjacent blanking ports 22 is the distance between two points closest to the two adjacent blanking ports 22 in the first direction, and the interval between two adjacent blanking ports 22 may be any value between 100mm and 300mm, for example, the interval between two adjacent blanking ports 22 may be 105mm, 159mm, 201.6mm, 300mm, and the like. Preferably, the spacing between two adjacent blanking openings 22 is 100mm, so that eight blanking openings 22 can be distributed on the distributor 2, thereby making the flow of the adsorbent particles more uniform.
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 distribution plate 21 has a length of 2000mm and the distribution plate 21 has a width of 1000mm, and is arranged such that the distribution plate 21 completely covers the cross section of the tower body 1, and all the adsorbent particles flow downward through the distribution plate 21.
In other embodiments, the distribution plate 21 may be circular, oval, triangular, etc.
In some embodiments, the down pipe 3 extends in a vertical direction, and the length of the down pipe 3 in the vertical direction is 500mm-700mm.
In some embodiments, the width of the upper end opening of the down pipe 3 is greater than or equal to the radius of the packing angle 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 comprises a first section 31 and a second section 32, the first section 31 having a width which is larger than the width of the second section 32, the lower end of the first section 31 being connected to the upper end of the second section 32.
In particular, the first section 31 of the down pipe 3 is located above the second section 32 of the down pipe 3, the first section 31 of the down pipe 3 is elongated in cross-section, the second section 32 of the down pipe 3 is elongated in cross-section, and the second section 32 of the down pipe 3 has a smaller cross-sectional area than the first section 31. Thus, the larger cross-sectional area of the first section 31 facilitates the adsorbent particles falling into the first section 31, and the smaller cross-sectional area of the second section 32 facilitates the control of the flow rate of the adsorbent particles out of the down pipe 3 to be the same as the flow rate of the adsorbent particles into the down pipe 3.
In some embodiments, the width of the first section 31 is 200mm to 400mm and the width of the second section 32 is 100mm to 200mm.
Specifically, the widths of the first section 31 and the second section 32 are the sizes of the first section 31 and the second section 32 along the first direction, the width of the first section 31 is the width of the upper end opening of the blanking pipe 3, the lengths of the first section 31 and the second section 32 are the sizes of the first section 31 and 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, and the length of the second section 32 may also be smaller than that of the first section 31. The width of the first section 31 is greater than the width of the second section 32.
Preferably, the first section 31 has a width of 290mm and the second section 32 has a width of 100mm, which are arranged such that the first section 31 can be fitted over the lower end of the distribution pipe 22.
In some embodiments, the flue gas inlet 131 is located above the bottom end of the down pipe 3.
In particular, the height of the lowermost end of the flue gas inlet 131 is higher than the height of the lower end of the down pipe 3. From this, gas inlet 131 is located the top of blanking pipe 3 lower extreme completely, when guaranteeing that the adsorbent falls down from blanking pipe 3, can not pass through gas inlet 131 spill tower body 1, has improved the efficiency that the adsorbent was collected.
In some embodiments, the cavity further includes a discharge section 14 located below the air outlet 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 next step's processing 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, and the like.
Preferably, the discharge section 14 has a height of 1.8m, so that the material flows smoothly downward.
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, so that the arrangement fully considers the height of a material bed and the occupied space.
In some embodiments, the height of gas inlet section 13 is 1.0m to 2.0m, the height of filler section 12 is 2.0m to 3.0m, and the height of gas outlet section 11 is 0.5m to 1m.
Specifically, the height of the packing section 12 is greater than the sum of the gas inlet section 13 and the gas outlet section 11, for example, the height of the gas inlet section 13 is 1.5m, the height of the gas outlet section 11 is 0.6m, and the height of the packing section 12 is 2.5m, so that, because the height of the packing section 12 is greater than the sum of the gas inlet section 13 and the gas outlet section 11, the retention time of the adsorbent in the packing section 12 is greater than the sum of the retention time in the gas inlet section 13 and the retention time in the gas outlet section 11, the adsorption time of the adsorbent on the flue gas is increased, and the adsorption efficiency is improved.
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 air outlet section 11 is 0.7m, so that the material can be distributed on the distributing plate 21.
In some embodiments, the moving bed adsorption column has a space velocity of 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 -1300h -1 The adsorption effect of the moving bed adsorption tower is optimized.
According to the embodiment of the invention, the flue gas purification system comprises: the smoke cooling device is provided with a smoke inlet and a smoke outlet and is used for cooling the smoke entering from the smoke inlet to room temperature or below; the moving bed adsorption tower is the moving bed adsorption tower in any of the above embodiments, the smoke outlet of the smoke cooling device is communicated with the smoke outlet 121 of the moving bed adsorption tower, and the moving bed adsorption tower is used for adsorbing smoke.
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 ℃). Alternatively, 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 components are usedLow temperature oxidation adsorption mechanism to NO 2 Adsorption 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%, and the denitration efficiency is obviously superior to 70-80% 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 implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such 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. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are exemplary and not to be construed as limiting the present invention, and that changes, 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 (12)
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 a gas inlet section, a filler section and a gas outlet section in the flowing direction of flue gas, and the filler 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 filler section so that the adsorbent in the filler section can flow out through the blanking ports;
the blanking device comprises a plurality of blanking pipes, a plurality of blanking pipes and a plurality of blanking ports in one-to-one correspondence, wherein the blanking pipes are located below the blanking ports and have intervals between the blanking ports so that smoke can flow conveniently, a smoke inlet is located below the blanking ports, the blanking pipes are located above discharge ports, the blanking ports are strip-shaped ports and a plurality of the blanking ports are arranged at intervals in a first direction, the blanking ports extend along a second direction, and the first direction and the second direction are perpendicular to each other.
2. The moving bed adsorption tower of claim 1, wherein the distributor comprises a distribution plate, the blanking port is disposed on the distribution plate, the distribution plate is connected to the peripheral wall of the cavity, and the flue gas inlet is located below the distribution plate.
3. The moving bed adsorption tower of claim 2, wherein 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.
4. The moving bed adsorption column according to claim 1, wherein the width of the drop opening is 80mm to 200mm, the size of the distributor in the second direction is L, and the size of the length of the drop opening is 0.8L to 0.95L.
5. The moving bed adsorption column according to claim 4, wherein the distance between two adjacent blanking ports is 100mm to 300mm.
6. The moving bed adsorption tower according to claim 2, wherein the distribution plate is rectangular, the length of the distribution plate is 1000mm to 3000mm, the width of the distribution plate is 500mm to 1500mm, the first direction is the length direction of the distribution plate, and the second direction is the width direction of the distribution plate.
7. A moving bed adsorption tower according to claim 1 wherein the drop tube extends in a vertical direction and the length of the drop tube in the vertical direction is 500mm to 700mm.
8. The moving bed adsorption column according to claim 1 or 7, wherein the width of the upper end opening of the down pipe is equal to or greater than the radius of the angle of repose of the adsorbent.
9. The moving bed adsorption column according to claim 8, wherein the drop tube comprises a first section and a second section, the first section having a width greater than a width of the second section, a lower end of the first section being connected to an upper end of the second section.
10. The moving bed adsorption column according to claim 9, wherein the width of the first section is from 200mm to 400mm and the width of the second section is from 100mm to 200mm.
11. The moving bed adsorption tower of claim 1, wherein the flue gas inlet is located above the bottom end of the down pipe.
12. 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 1-11, 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2022/106389 WO2023029781A1 (en) | 2021-09-02 | 2022-07-19 | Moving bed adsorption tower with distributor and flue gas purification system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2021110285178 | 2021-09-02 | ||
| CN202111028517 | 2021-09-02 |
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| CN113828111A CN113828111A (en) | 2021-12-24 |
| CN113828111B true CN113828111B (en) | 2023-02-24 |
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| CN202111082809.XA Active CN113828111B (en) | 2021-09-02 | 2021-09-15 | Moving bed adsorption tower with distributor and flue gas purification system |
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| CN (1) | CN113828111B (en) |
| WO (1) | WO2023029781A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113797711B (en) * | 2021-09-02 | 2023-06-06 | 中国华能集团有限公司 | Moving bed adsorption tower and flue gas purification system |
| CN113828111B (en) * | 2021-09-02 | 2023-02-24 | 中国华能集团有限公司 | Moving bed adsorption tower with distributor and flue gas purification system |
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| WO1996024432A1 (en) * | 1995-02-10 | 1996-08-15 | Kovinska Industrija Vransko | Flue gas purification apparatus |
| CN103230723A (en) * | 2013-04-22 | 2013-08-07 | 西安热工研究院有限公司 | Annular sectional cross-flow fume cleaning adsorption tower |
| CN111841240A (en) * | 2019-04-26 | 2020-10-30 | 英特佳工程与环境技术有限公司 | Container and method for loading ammonia gas into adsorbent and/or absorbent |
| CN113144825A (en) * | 2021-06-06 | 2021-07-23 | 国电环境保护研究院有限公司 | Multi-cycle adsorption tower for industrial tail gas treatment |
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| DE3732567A1 (en) * | 1987-05-07 | 1988-11-24 | Horst Dr Grochowski | ANSTROME FLOOR FOR WALKING BED REACTORS AND METHOD FOR OPERATING THIS DEVICE |
| DE3916325A1 (en) * | 1989-05-19 | 1990-11-22 | Grochowski Horst | WALKING BED REACTOR |
| CN107661681A (en) * | 2017-11-08 | 2018-02-06 | 中国科学院过程工程研究所 | A kind of flue gas pollutant purifying column |
| CN113828109B (en) * | 2021-09-02 | 2023-03-07 | 中国华能集团有限公司 | Flue gas purification system and moving bed adsorption tower with distributor thereof |
| CN113797710B (en) * | 2021-09-02 | 2023-10-20 | 中国华能集团有限公司 | Flue gas purification system and moving bed adsorption tower thereof |
| CN113828108B (en) * | 2021-09-02 | 2023-03-10 | 中国华能集团有限公司 | Flue gas purification system and moving bed adsorption tower |
| CN113828110B (en) * | 2021-09-02 | 2023-01-31 | 中国华能集团有限公司 | Moving bed adsorption tower and flue gas purification system with same |
| CN113828111B (en) * | 2021-09-02 | 2023-02-24 | 中国华能集团有限公司 | Moving bed adsorption tower with distributor and flue gas purification system |
| CN113828112B (en) * | 2021-09-02 | 2023-05-09 | 中国华能集团有限公司 | Moving bed adsorption tower and flue gas purification system |
| CN113797712B (en) * | 2021-09-02 | 2023-02-28 | 中国华能集团有限公司 | Flue gas purification system and moving bed adsorption tower |
-
2021
- 2021-09-15 CN CN202111082809.XA patent/CN113828111B/en active Active
-
2022
- 2022-07-19 WO PCT/CN2022/106389 patent/WO2023029781A1/en unknown
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1996024432A1 (en) * | 1995-02-10 | 1996-08-15 | Kovinska Industrija Vransko | Flue gas purification apparatus |
| CN103230723A (en) * | 2013-04-22 | 2013-08-07 | 西安热工研究院有限公司 | Annular sectional cross-flow fume cleaning adsorption tower |
| CN111841240A (en) * | 2019-04-26 | 2020-10-30 | 英特佳工程与环境技术有限公司 | Container and method for loading ammonia gas into adsorbent and/or absorbent |
| CN113144825A (en) * | 2021-06-06 | 2021-07-23 | 国电环境保护研究院有限公司 | Multi-cycle adsorption tower for industrial tail gas treatment |
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| Publication number | Publication date |
|---|---|
| CN113828111A (en) | 2021-12-24 |
| WO2023029781A1 (en) | 2023-03-09 |
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