CN113797712B - 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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- CN113797712B CN113797712B CN202111082826.3A CN202111082826A CN113797712B CN 113797712 B CN113797712 B CN 113797712B CN 202111082826 A CN202111082826 A CN 202111082826A CN 113797712 B CN113797712 B CN 113797712B
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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
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 a gas inlet section, a filler section and a gas outlet 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 so that the adsorbent in the filling section can flow out through the blanking inlets and the corresponding blanking outlets; the blanking pipes correspond to the blanking outlets one by one, the blanking outlets are positioned in the blanking pipes, the flue gas inlet is positioned below the blanking inlet, and the blanking pipes are positioned above the discharge port. 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 harming the atmospheric environment and human health. The fixed bed adsorption tower is adopted usually in the gas cleaning field to adsorb the purpose in order to realize purifying flue gas to the pollutant in the flue gas, but fixed bed adsorption tower among the correlation technique ubiquitous filler layer pressure and density when using problem that reduces along with the live time extension that adsorb effect is uneven, adsorption effect is poor, adsorption efficiency seriously influences the adsorption efficiency when needing to change the adsorbent moreover, 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 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 according to an embodiment of the present invention includes: 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 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 so that the adsorbent in the filling section can flow out through the blanking inlets and the corresponding blanking outlets; the device comprises a plurality of blanking pipes, wherein the blanking pipes correspond to the blanking outlets one to one, the blanking outlets are located in the blanking pipes, a gap is formed between each blanking pipe and the corresponding distributor so that smoke can pass through the gap, the smoke inlet is located below the blanking inlet, and the blanking pipes are located above the discharge port.
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 includes distribution plate and a plurality of distribution pipe, the blanking entry is established on the distribution plate, the distribution pipe with the lower terminal surface of distribution plate links to each other and follows the distribution plate downwardly extending, and is a plurality of the distribution pipe is with a plurality of blanking entry one-to-one, the lower extreme of distribution pipe is equipped with the blanking export, and is a plurality of the blanking pipe is with a plurality of the distribution pipe one-to-one, the lower tip of distribution pipe stretches into the correspondence in the upper end of blanking pipe, the top of blanking pipe with the lower terminal surface of distribution plate has the gap between, the distribution pipe with the correspondence have the interval between the blanking pipe, flue gas inlet is located the below of 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 50mm to 100mm.
In some embodiments the distribution pipe has an outer circumferential wall spaced from the inner circumferential wall of the down pipe by 50-100 mm in the horizontal direction.
In some embodiments, the length of the portion of the distribution pipe extending into the blanking pipe is 10mm-40mm.
In some embodiments, the blanking inlets are strip-shaped openings, a plurality of the blanking inlets are arranged at intervals in a first direction, the blanking inlets extend along a second direction, and the first direction and the second direction are perpendicular to each other.
In some embodiments, the width of the blanking inlet is 80mm-200mm, the dimension of the distributor in the second direction is L, and the length of the blanking inlet is 0.8L-0.95L.
In some embodiments, the interval between two adjacent blanking inlets 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 down pipe comprises a first section and a second section, the width of the first section is larger than the width of the second section, the lower end of the first section is connected with the upper end of the second section, and the lower end of the distribution pipe extends into the corresponding first section of the down pipe.
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.
A flue gas purification system according to an embodiment of the present invention includes: 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 moving bed adsorption tower, wherein the moving bed adsorption tower is according to any one of the embodiments, a flue gas outlet of the flue gas cooling device 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 flue gas outlet 112; a filler section 12; 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; the distribution pipe 22; a blanking inlet 221; a blanking outlet 222;
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 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 112 which are communicated with the cavity, the cavity is provided with an air inlet section 13, a filler section 12 and an air 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 112 is communicated with the gas outlet section 11, the charging opening 111 and the flue gas outlet 112 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 smoke flowing direction is from the smoke inlet 131 to the smoke outlet 112, and the air outlet section 11, the filler section 12 and the air inlet end are sequentially arranged along the direction from top to bottom. From this, the flue gas gets into the inside of tower body 1 and flows from the upside of tower body 1 from the lower half of tower body 1, the adsorbent gets into tower body 1 and flows from the lower extreme of tower body 1 from the upside of tower body 1, 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 the gas outlet 112 exhaust gas, and the adsorption efficiency is improved.
The distributor 2 is arranged in the tower body 1, the distributor 2 comprises a plurality of blanking inlets 221 and a plurality of blanking outlets 222 corresponding to the blanking inlets 221, and the distributor 2 is positioned below the packing section 12 so that the adsorbent in the packing section 12 flows out through the blanking inlets 221 and the corresponding blanking outlets 222.
Specifically, the blanking outlets 222 correspond to the blanking inlets 221 one by one, the blanking outlets 222 are located below the blanking inlets 221, and the blanking inlets 221 are arranged in parallel at intervals and have equal intervals. Therefore, the adsorbent passes through the blanking inlet 221 and the blanking outlet 222 to enter the blanking pipe 3, the flow of the adsorbent passing through the uniformly arranged blanking inlet 221 is approximately the same, on one hand, the downward flowing speed of the adsorbent is delayed, the contact time of the adsorbent particles and the flue gas is increased, on the other hand, the adsorbent is prevented from flowing out from one or more distribution pipes 22 in a concentrated manner and generating dead angles in the flowing process, the flowing efficiency of the adsorbent is improved, and the adsorption effect is improved.
The plurality of blanking pipes 3 correspond to the plurality of blanking outlets 222 one by one, the blanking outlets 222 are located in the blanking pipes 3, a gap is formed between the blanking pipes 3 and the distributor 2 so that smoke can pass through the gaps, the smoke inlet 131 is located below the blanking inlet 221, and the blanking pipes 3 are located above the discharge ports 141.
Specifically, the lower end of the blanking outlet 222 extends into the blanking pipe 3, and the gap between the blanking pipe 3 and the distributor 2 is the gap between the upper end of the inner wall of the blanking pipe 3 and the lower end of the outer wall of the blanking outlet 222. From this, when passing blanking outlet 222 and falling into blanking pipe 3, the adsorbent can fall into blanking pipe 3 completely, avoids the adsorbent to follow the clearance spill between blanking outlet 222 and the blanking pipe 3 to avoid the adsorbent to flow out tower body 1 from flue gas inlet 131.
In some embodiments, the distributor 2 includes a distribution plate 21 and a plurality of distribution pipes 22, the blanking inlets 221 are disposed on the distribution plate 21, the distribution pipes 22 are connected to a lower end surface of the distribution plate 21 and extend downward from the distribution plate 21, the plurality of distribution pipes 22 are in one-to-one correspondence with the plurality of blanking inlets 221, the lower end of the distribution pipe 22 is provided with a blanking outlet 222, the plurality of blanking pipes 3 are in one-to-one correspondence with the plurality of distribution pipes 22, the lower end portions of the distribution pipes 22 extend into upper end portions of the corresponding blanking pipes 3, a gap is formed between the top end of the blanking pipe 3 and the lower end surface of the distribution plate 21, a gap is formed between the distribution pipe 22 and the corresponding blanking pipe 3, and the flue gas inlet 131 is located below the distribution plate 21.
Specifically, 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 at equal intervals, the cross section of the distribution pipe 22 is long, the distribution pipe 22 extends along the vertical direction, and the cross section of the distribution pipe 22 is reduced along the direction from top to bottom. Therefore, the adsorbent can uniformly flow out of the distributor 2, so that dead angles are avoided in the flow, and the adsorption efficiency is improved. The geometric centre of the distribution pipe 22 coincides with the geometric centre of the down pipe 3. From this, the adsorbent that flows out among the distribution pipe 2 can directly fall into blanking pipe 3, has avoided the adsorbent to flow smoothly from distributor 2 entering blanking pipe 3 and has led to the fact and pile up, has improved the smooth degree that the adsorbent flows in the inner chamber.
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 50mm to 100mm. Specifically, the above dimension may be any value between 50mm and 100mm, for example, the dimension of the gap between the top end of the down pipe 3 and the lower end face of the distribution plate 21 in the vertical direction may be 53mm, 60mm, 70.5mm, 88m, or the like.
Preferably, the gap between the top end of the down pipe 3 and the lower end face of the distribution plate 21 has a dimension of 95mm in the vertical direction, so that the flow rate required for the air passing through the gap to reach the space velocity of the adsorption tower is set.
In some embodiments the distribution pipe 22 has an outer circumferential wall horizontally spaced from the inner circumferential wall of the corresponding down pipe 3 by 50-100 mm. Specifically, the dimension may be any value between 50mm and 100mm, for example, the dimension of the gap between the top end of the down pipe 3 and the lower end surface of the distribution plate 21 in the vertical direction may be 53mm, 60mm, 70.5mm, 88m, or the like.
Preferably, the distribution pipe 22 has an outer peripheral wall spaced from the corresponding inner peripheral wall of the down pipe 3 by 95mm in the horizontal direction, so that the flow rate of air passing through the gap is set to achieve the space velocity of the adsorption tower.
In some embodiments the length of the portion of the distribution pipe 22 that protrudes into the down pipe 3 is between 10mm and 40mm. Specifically, the length of the portion of the distribution pipe 22 extending into the blanking pipe 3 is the distance between the bottom end of the blanking outlet 222 and the upper end of the blanking pipe 3 in the vertical direction, and the length of the portion of the distribution pipe 22 extending into the blanking pipe 3 may be any value between 10mm and 40mm, for example, the length of the portion of the distribution pipe 22 extending into the blanking pipe 3 may be 15mm, 20.5mm, 36mm, 40mm, and the like.
Preferably, the length of the part of the distribution pipe 22 that protrudes into the down pipe 3 is 25mm, which is arranged to ensure air circulation while also effectively preventing sorbent particles from splashing out of the distribution pipe and down pipe.
In some embodiments, the blanking inlets 221 are bar-shaped openings, the plurality of blanking inlets 221 are spaced in a first direction, the blanking inlets 221 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 a left-right direction, the second direction is a front-back direction, and the blanking inlets 221 are arranged at equal intervals along the first direction, so that the blanking inlets 221 are elongated, which not only can bundle the adsorbent particles into the distribution pipe 22, but also can ensure a larger cross-sectional area of the blanking inlets 221, thereby ensuring the flowability of the adsorbent particles.
In other embodiments, the blanking inlet 221 can be circular, triangular, diamond-shaped, etc.
In some embodiments, the width of the blanking inlet 221 is 80mm-200mm, the dimension of the distributor 2 in the second direction is L, and the length of the blanking inlet 221 is 0.8L-0.95L. Specifically, the width of the blanking inlet 221 may be any value between 80mm and 200mm, for example, the width of the blanking inlet 221 may be 85mm, 100mm, 151.8mm, 200mm, and the like. Preferably, the width of the blanking inlet 221 is 290mm, which is set to achieve the design requirement of the flow rate of the adsorbent particles through the blanking inlet 221.
It should be noted that the width of the blanking inlet 221 is the size of the blanking inlet 221 in the first direction, and the length of the blanking inlet 221 is the size of the blanking inlet 221 in the second direction.
Preferably, the size of the distributor 2 in the second direction is 1850mm, and the length of the blanking inlet 221 is 900mm, so that the flow rate of the adsorbent particles flowing through the blanking inlet 221 is designed.
In some embodiments, the spacing between two adjacent blanking inlets 221 is 100mm-300mm. Specifically, the interval between two adjacent blanking inlets 221 is the distance between two points closest to the two adjacent blanking inlets 221 in the first direction, and the interval between two adjacent blanking inlets 221 may be any value between 100mm and 300mm, for example, the interval between two adjacent blanking inlets 221 may be 105mm, 159mm, 201.6mm, 300mm, and the like. Preferably, the interval between two adjacent blanking inlets 221 is 100mm, so that eight blanking inlets 221 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 comprises a first section 31 and a second section 32, the width of the first section 31 being 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, and the lower end of the distribution pipe 22 extending into the corresponding first section 31 of the down pipe 3.
Specifically, the first section 31 of the down pipe 3 is located above the second section 32 of the down pipe 3, the cross section of the first section 31 of the down pipe 3 is elongated, the cross section of the second section 32 of the down pipe 3 is elongated, and the cross section of the second section 32 of the down pipe 3 is smaller than the first section 31 of the down pipe 3. Therefore, the larger cross-sectional area of the first section 31 facilitates the extension of the discharging outlet 222 into the first section 31, and the inner wall of the first section 31 can keep a distance from the outer wall of the discharging outlet 222 to form a gap for the flowing of the flue gas.
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 segment 31 and the second segment 32 are the sizes of the first segment 31 and the second segment 32 along the first direction, the lengths of the first segment 31 and the second segment 32 are the sizes of the first segment 31 and the second segment 32 along the second direction, the length of the second segment 32 may be equal to that of the first segment 31, and the length of the second segment 32 may be smaller than that of the first segment 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 290 and the second section 32 has a width 100, 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 lower end of the down pipe 3.
Specifically, 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. From this, gas inlet 131 is located the top of the lower extreme of blanking pipe 3 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 gas 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 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 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 moving bed adsorption column may have 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, since 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 for 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, and the arrangement can reduceThe volume of the adsorption tower of the moving bed can also reduce the filling amount of the adsorbent in the tower.
Preferably, the space velocity of the adsorption tower of the moving bed is 1000h -1 -1200h -1 The adsorption effect of the moving bed adsorption tower is optimized.
A flue gas purification system according to an embodiment of the present invention includes: 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 the room temperature or below; the flue gas cooling device is connected with the flue gas outlet 112 of the moving bed adsorption tower, and the moving bed adsorption tower is used for adsorbing the flue gas.
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 adsorbed physically, so that 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 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, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of 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 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 explicitly stated or limited, the terms "mounted," "connected," "fixed," and the like are to be construed broadly, e.g., as being permanently connected, detachably connected, or integral; 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 expressly stated or limited otherwise, the first feature "on" or "under" the second feature may be directly contacting the second feature or the first and second features may be indirectly contacting each other through intervening media. 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 "under," "beneath," and "under" a second feature may be directly under or obliquely under the second 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," "an example," "a specific example," or "some examples" and the like mean that a specific 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 (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 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 so that the adsorbent in the filling section can flow out through the blanking inlets and the corresponding blanking outlets;
the blanking device comprises a plurality of blanking pipes, wherein the blanking pipes correspond to the blanking outlets one to one, the blanking outlets are located in the blanking pipes, gaps are formed between the blanking pipes and a distributor so that smoke can pass through the blanking pipes, a smoke inlet is located below a blanking inlet, the blanking pipes are located above a discharge port, the blanking inlet is a strip-shaped opening and is arranged at intervals in a first direction, the blanking inlet extends along a second direction, and the first direction is perpendicular to the second direction.
2. A moving bed adsorption tower according to claim 1 wherein the distributor comprises a distribution plate and a plurality of distribution pipes, the drop inlet is provided on the distribution plate, the distribution pipes are connected to the lower end surface of the distribution plate and extend downward from the distribution plate, the plurality of distribution pipes are in one-to-one correspondence with the plurality of drop inlets, the lower end of the distribution pipes is provided with the drop outlet, the plurality of drop pipes are in one-to-one correspondence with the plurality of distribution pipes, the lower end portions of the distribution pipes extend into the upper end portions of the corresponding drop pipes, gaps are provided between the top ends of the drop pipes and the lower end surface of the distribution plate, the distribution pipes are spaced from the corresponding drop pipes, and the flue gas inlet is located below the distribution plate.
3. The moving bed adsorption tower according to claim 2, wherein a gap between the top end of the down pipe and the lower end surface of the distribution plate has a vertical dimension of 50mm to 100mm.
4. The moving bed adsorption column according to claim 2, wherein the outer peripheral wall of the distribution pipe is horizontally spaced from the inner peripheral wall of the corresponding down pipe by 50mm to 100mm.
5. A moving bed adsorption tower according to any one of claims 2 to 4 wherein the length of the portion of the distribution pipe projecting into the drop pipe is from 10mm to 40mm.
6. A moving bed adsorption tower according to claim 1, wherein the width of the drop inlet is 80mm to 200mm, the dimension of the distributor in the second direction is L, and the length of the drop inlet is 0.8L to 0.95L.
7. The moving bed adsorption tower of claim 1, wherein the spacing between adjacent two of the drop inlets is in the range of 100mm to 300mm.
8. The moving bed adsorption tower of 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.
9. The moving bed adsorption tower according to claim 2, wherein the down pipe comprises a first section and a second section, the width of the first section is greater than the width of the second section, the lower end of the first section is connected with the upper end of the second section, and the lower end of the distribution pipe extends into the corresponding first section of the down pipe.
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 column according to claim 1, wherein the flue gas inlet is located above the bottom end of the down pipe.
12. A flue gas cleaning 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 to 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.
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| CN202111028509 | 2021-09-02 | ||
| CN2021110285093 | 2021-09-02 |
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| US5356462A (en) * | 1990-10-16 | 1994-10-18 | Steag Aktiengesellschaft | Adsorption medium reactor, espectially fluidized bed reactor |
| WO1996024432A1 (en) * | 1995-02-10 | 1996-08-15 | Kovinska Industrija Vransko | Flue gas purification apparatus |
| 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 |
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|---|---|---|---|---|
| WO1990011815A1 (en) * | 1989-03-30 | 1990-10-18 | Nymic Anstalt | Reactor module |
| US5356462A (en) * | 1990-10-16 | 1994-10-18 | Steag Aktiengesellschaft | Adsorption medium reactor, espectially fluidized bed reactor |
| WO1996024432A1 (en) * | 1995-02-10 | 1996-08-15 | Kovinska Industrija Vransko | Flue gas purification apparatus |
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