CN113828109A - Flue gas purification system and moving bed adsorption tower with distributor thereof - Google Patents

Flue gas purification system and moving bed adsorption tower with distributor thereof Download PDF

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Publication number
CN113828109A
CN113828109A CN202111081488.1A CN202111081488A CN113828109A CN 113828109 A CN113828109 A CN 113828109A CN 202111081488 A CN202111081488 A CN 202111081488A CN 113828109 A CN113828109 A CN 113828109A
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blanking
flue gas
section
inlets
pipes
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CN113828109B (en
Inventor
牛红伟
汪世清
许世森
梁鹤涛
郜时旺
肖平
刘练波
虢德军
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Huaneng Clean Energy Research Institute
China Huaneng Group Co Ltd
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Huaneng Clean Energy Research Institute
China Huaneng Group Co Ltd
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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
    • 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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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

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

Description

Flue gas purification system and moving bed adsorption tower with distributor thereof
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 with a distributor.
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 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 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 feeding port, a discharging port, 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 comprises a plurality of blanking inlets and a plurality of blanking outlets corresponding to the blanking inlets, 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, and the blanking inlets are square; 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, the distribution pipe is square pipe, 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 correspond the interval has between the blanking pipe, flue gas inlet is located the below of 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 outer circumferential wall of the distribution pipe is horizontally spaced from the inner circumferential wall of the corresponding down pipe by 5mm to 40 mm.
In some embodiments, the length of the part of the distribution pipe extending into the blanking pipe is 5mm-40mm
In some embodiments, the plurality of blanking inlets are arranged in multiple rows, each row of blanking inlets includes a plurality of blanking inlets, the plurality of blanking inlets in each row of blanking inlets are arranged at intervals along a first direction, the multiple rows of blanking inlets 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 inlets are aligned along the second direction.
In some embodiments, the edge of the blanking inlet is square, and the side of the blanking inlet is 150mm-300 mm.
In some embodiments, the interval between two adjacent blanking inlets in the first direction is 20mm-100mm, and the interval between two adjacent blanking inlets in the second direction is 20mm-100 mm.
In some embodiments, the down pipe is a circular pipe, the down pipe includes a first section and a second section, the diameter of the first section is larger than that 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 first section of the down pipe correspondingly.
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 moving bed adsorption tower, the moving bed adsorption tower is the moving bed adsorption tower in 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 is a cross-sectional view at a-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 a plurality of down tubes of fig. 3.
FIG. 7 is a schematic cross-sectional view of a plurality of down tubes in another embodiment.
Reference numerals:
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; the distribution pipe 22; a blanking inlet 23; a blanking outlet 24;
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 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 smoke flowing direction is from the smoke inlet 131 to the smoke 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 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 121 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 23 and a plurality of blanking outlets 24 corresponding to the blanking inlets 23, 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 23 and the corresponding blanking outlets 24, wherein the blanking inlets 23 are square;
specifically, the blanking outlets 24 correspond to the blanking inlets 23 one by one, the blanking outlets 24 are located below the blanking inlets 23, and the blanking inlets 23 are arranged in parallel at intervals and have equal intervals. Therefore, the adsorbent passes through the blanking inlet 23 and the blanking outlet 24 to enter the blanking pipe 3, the flow of the adsorbent passing through the uniformly arranged blanking inlet 23 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 mode and generating dead angles in the flowing process, the flowing efficiency of the adsorbent is improved, and the adsorption effect is improved.
The blanking pipes 3 correspond to the blanking outlets 24 one by one, the blanking outlets 24 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 gap, the smoke inlet 131 is located below the blanking inlet 23, and the blanking pipes 3 are located above the discharge ports 141.
Specifically, the lower end of the blanking outlet 24 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 24. From this, when passing blanking outlet 24 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 24 and the blanking pipe 3 to avoid the adsorbent to flow out tower body 1 from flue gas import 131.
In some embodiments, the distributor 2 includes a distribution plate 21 and a plurality of distribution pipes 22, the blanking inlets 23 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 distribution pipes 22 are square pipes, the plurality of distribution pipes 22 are in one-to-one correspondence with the plurality of blanking inlets 23, the lower ends of the distribution pipes 22 are provided with blanking outlets 24, the plurality of blanking pipes 3 are in one-to-one correspondence with the plurality of distribution pipes 22, the lower ends of the distribution pipes 22 extend into upper ends of the corresponding blanking pipes 3, gaps are formed between top ends of the blanking pipes 3 and the lower end surface of the distribution plate 21, intervals are formed between the distribution pipes 22 and the corresponding blanking pipes 3, and the smoke inlets 131 are located below the distribution plate 21.
Specifically, as shown in fig. 5, the distribution plate 21 is provided with through holes having the same shape as the distribution pipes 22, the through holes are arranged in parallel at equal intervals, the cross section of the distribution pipe 22 is square, and the distribution pipe 22 extends in the vertical direction. Note that the blanking inlet 23 and the blanking outlet 24 are both square. 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 in the horizontal direction coincides with the geometric centre of the down pipe 3 in the horizontal direction. From this, the adsorbent that flows out among the distribution pipe 222 can directly fall into down pipe 3, has avoided the adsorbent to flow smoothly from distributor 2 entering down 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 20mm to 100 mm. Specifically, the above dimension may be any value between 20mm and 100mm, and 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 33mm, 40mm, 60.5mm, 88m, or the like.
Preferably, the size of the gap between the top end of the blanking pipe 3 and the lower end face of the distribution plate 21 in the vertical direction is 35mm, so that the setting reduces the path length of the flue gas passing between the distribution pipe 22 and the blanking pipe 3, the flue gas flows more smoothly, the distribution pipe 22 can conveniently extend into the interior of the blanking pipe 3, the adsorbent particles are prevented from splashing out of the tower body 1 through the gap between the distribution pipe 22 and the blanking pipe 3, and the loss of the adsorbent is reduced.
In some embodiments, the outer circumferential wall of the distribution pipe 22 is horizontally spaced from the inner circumferential wall of the corresponding down pipe 3 by 5mm to 40 mm. In particular, the dimension may be any value between 50mm and 100mm, for example, the spacing between the outer peripheral wall of the distribution pipe 22 and the inner peripheral wall of the corresponding down pipe 3 in the horizontal direction may be 9mm, 15.5mm, 26mm, 40mm, etc.
Preferably, the interval is 25mm in the horizontal direction between the periphery wall of distribution pipe 22 and the interior perisporium of corresponding blanking pipe 3, has set up like this and has reduced the path length that the flue gas passed through between distribution pipe 22 and the blanking pipe 3, makes the flue gas flow more smooth, and on the other hand distribution pipe 22 of being convenient for stretches into the inside of blanking pipe 3, prevents that the adsorbent granule from spilling tower body 1 through the space between distribution pipe 22 and the blanking pipe 3, has reduced the loss of adsorbent.
In some embodiments the length of the portion of the distribution pipe 22 that protrudes into the down pipe 3 is 5-40 mm. 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 24 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 5mm and 40mm, for example, the length of the portion of the distribution pipe 22 extending into the blanking pipe 3 may be 9mm, 15.5mm, 26mm, 40mm, and the like.
Preferably, the length of the part of the distribution pipe 22 extending into the blanking pipe 3 is 25mm, so that the path length of the flue gas passing between the distribution pipe 22 and the blanking pipe 3 is reduced, the flue gas flows more smoothly, and the distribution pipe 22 extending into the blanking pipe 3 can effectively prevent the adsorbent particles from splashing out of the tower body 1 through the gap between the distribution pipe 22 and the blanking pipe 3, thereby reducing the loss of the adsorbent.
In some embodiments, the plurality of blanking inlets 23 are arranged in a plurality of rows, each row of blanking inlets 23 includes a plurality of blanking inlets 23, the plurality of blanking inlets 23 in each row of blanking inlets 23 are spaced apart along a first direction, the plurality of rows of blanking inlets 23 are spaced apart along a second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of blanking inlets 23 are aligned along the second direction.
Specifically, 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. As shown in fig. 4, the first direction is a left-right direction, and the second direction is a front-back direction.
Preferably, the distribution plate 21 has a length of 2000mm and the distribution plate 21 has a width of 1000mm, which is arranged to facilitate the fixing of the distribution plate 21 to the tower 1.
In other embodiments, the distribution plate 21 may be circular, oval, triangular, etc.
In some embodiments, the edge of the blanking inlet 23 is square, and the side of the blanking inlet 23 is 150mm-300 mm. Specifically, the side length of the blanking inlet 23 may be any value between 150mm and 300mm, for example, the side length of the blanking inlet 23 may be 160mm, 199.5mm, 266mm, 299mm, and the like.
Preferably, the side length of the material dropping inlet 23 is 200mm, so that more material dropping inlets 23 can be arranged on the distribution plate 21.
In some embodiments, the interval between two adjacent blanking inlets 23 in the first direction is 20mm-100mm, and the interval between two adjacent blanking inlets 23 in the second direction is 20mm-100 mm.
Specifically, the interval between two adjacent blanking inlets 23 is the distance between the nearest two points of the two adjacent blanking inlets 23. The interval between two adjacent blanking inlets 23 in the first direction may be the same as or different from the interval between two adjacent blanking inlets 23 in the second direction.
Preferably, the interval between two adjacent blanking inlets 23 in the first direction is 50mm, and the interval between two adjacent blanking inlets 23 in the second direction is 50mm.
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, and the lower end of the distribution pipe 22 extending into the corresponding first section 31 of the down pipe 3.
Specifically, the width of the first segment 31 and the second segment 32 is the size of the first segment 31 and the second segment 32 along the first direction, the length of the first segment 31 and the second segment 32 is the size 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 the length of the first segment 31, and the length of the second segment 32 may also be smaller than the length of the first segment 31. The width of the first section 31 is greater than the width of the second section 32. As shown in fig. 6, the down pipe 3 is a circular pipe for easy processing.
In other embodiments, as shown in fig. 7, the down pipe 3 may be a square pipe.
In some embodiments, the down pipe 3 extends in a vertical direction, the length of the down pipe 3 being 500mm-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 length of the down pipe 3 is 740mm, so that the material can smoothly flow downwards
In some embodiments, the flue gas inlet 131 is located above the drop outlet 24.
Specifically, the height of the lowermost end of the flue gas inlet 131 is higher than the height of the blanking outlet 24. From this, gas inlet 131 is located blanking outlet 24's top 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 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 3.0 m. 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 8.0 m. 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, and the like.
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 intake section 13 is 1.0m to 2.0m, the height of the filler section 12 is 2.0m to 3.0m, and the height of the cloth section 11 is 0.5m to 1 m.
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 material distribution section 11 is 0.7m, so that the material can be distributed on the material distribution plate 21.
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 moving bed adsorption tower is 1200h-1-1500h-1The adsorption effect of the moving bed adsorption tower is optimized.
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 the room temperature or below; the moving bed adsorption tower is the moving bed adsorption tower according to any one of the 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 gasxThe component is oxidized into NO by a low-temperature oxidation adsorption mechanism2Adsorption removal without spraying NH3The 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 gasxThe adsorption ratio is more than 99%, and the denitration efficiency is obviously superior to 70-80% 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 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 connected internally or in any other suitable relationship, unless expressly stated otherwise. 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," "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. 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 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 (10)

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 comprises a plurality of blanking inlets and a plurality of blanking outlets corresponding to the blanking inlets, 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, and the blanking inlets are square;
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.
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 formed in 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 distribution pipes are square pipes, the distribution pipes are in one-to-one correspondence with the drop inlets, the lower end of the distribution pipes is provided with the drop outlet, the drop pipes are in one-to-one correspondence with the distribution pipes, the lower end portions of the distribution pipes extend into the upper end portions of the corresponding drop pipes, gaps are formed 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 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 2, wherein the outer peripheral wall of the distribution pipe is horizontally spaced from the inner peripheral wall of the corresponding down pipe by 5mm to 40 mm.
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 5mm to 40 mm.
6. A moving bed adsorption tower according to any one of claims 1 to 4 wherein a plurality of said drop inlets are arranged in a plurality of rows, each row of drop inlets comprises a plurality of said drop inlets, the plurality of drop inlets in each row of drop inlets are spaced apart in a first direction, the plurality of rows of drop inlets are spaced apart in a second direction, the first direction and the second direction are perpendicular to each other, and two adjacent rows of drop inlets are aligned in the second direction.
7. The moving bed adsorption tower of claim 6, wherein the edges of the drop inlet are square and the sides of the drop inlet are 150mm-300mm long.
8. A moving bed adsorption tower according to claim 6, wherein the spacing between two adjacent drop inlets in the first direction is 20mm to 100mm, and the spacing between two adjacent drop inlets in the second direction is 20mm to 100 mm.
9. The moving bed adsorption tower of claim 2, wherein the down pipe is a circular pipe, the down pipe comprises a first section and a second section, the diameter of the first section is larger than that 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. 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 1-9, 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.
CN202111081488.1A 2021-09-02 2021-09-15 Flue gas purification system and moving bed adsorption tower with distributor thereof Active CN113828109B (en)

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Cited By (2)

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Publication number Priority date Publication date Assignee Title
WO2023029781A1 (en) * 2021-09-02 2023-03-09 中国华能集团清洁能源技术研究院有限公司 Moving bed adsorption tower with distributor and flue gas purification system
CN116351197A (en) * 2023-06-01 2023-06-30 中国华能集团清洁能源技术研究院有限公司 Flue gas distributor, adsorption tower and low-temperature flue gas adsorption system

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WO1988008746A1 (en) * 1987-05-07 1988-11-17 Horst Grochowski Feed inlet floor for mobile bed reactors
CN203002168U (en) * 2012-12-13 2013-06-19 成都源创环保工程有限公司 Moving bed adsorption tower for exhaust gas purification
CN207614615U (en) * 2017-12-07 2018-07-17 国电科学技术研究院 A kind of activated coke smoke eliminator of sulphur nitre integration removing

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Publication number Priority date Publication date Assignee Title
WO1988008746A1 (en) * 1987-05-07 1988-11-17 Horst Grochowski Feed inlet floor for mobile bed reactors
CN203002168U (en) * 2012-12-13 2013-06-19 成都源创环保工程有限公司 Moving bed adsorption tower for exhaust gas purification
CN207614615U (en) * 2017-12-07 2018-07-17 国电科学技术研究院 A kind of activated coke smoke eliminator of sulphur nitre integration removing

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023029781A1 (en) * 2021-09-02 2023-03-09 中国华能集团清洁能源技术研究院有限公司 Moving bed adsorption tower with distributor and flue gas purification system
CN116351197A (en) * 2023-06-01 2023-06-30 中国华能集团清洁能源技术研究院有限公司 Flue gas distributor, adsorption tower and low-temperature flue gas adsorption system
CN116351197B (en) * 2023-06-01 2023-08-29 中国华能集团清洁能源技术研究院有限公司 Flue gas distributor, adsorption tower and low-temperature flue gas adsorption system

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