WO2023029781A1 - 具有分布器的移动床吸附塔和烟气净化系统 - Google Patents

具有分布器的移动床吸附塔和烟气净化系统 Download PDF

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Publication number
WO2023029781A1
WO2023029781A1 PCT/CN2022/106389 CN2022106389W WO2023029781A1 WO 2023029781 A1 WO2023029781 A1 WO 2023029781A1 CN 2022106389 W CN2022106389 W CN 2022106389W WO 2023029781 A1 WO2023029781 A1 WO 2023029781A1
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Prior art keywords
flue gas
section
moving bed
adsorption tower
distributor
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PCT/CN2022/106389
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English (en)
French (fr)
Inventor
肖平
汪世清
许世森
王兴俊
郜时旺
刘练波
牛红伟
谢燮林
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中国华能集团清洁能源技术研究院有限公司
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Publication of WO2023029781A1 publication Critical patent/WO2023029781A1/zh

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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

Definitions

  • the present 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.
  • the related technology adopts the moving bed adsorption tower to make the adsorbent flow in the tower, so as to overcome the problem that the adsorption capacity of the fixed bed adsorption tower decreases with the prolongation of use time, but there are still uneven distribution of flue gas and poor purification effect in the moving bed adsorption tower. Ideal question.
  • the present invention aims to solve one of the technical problems in the related art at least to a certain extent. For this reason, the embodiment of the present invention proposes a moving bed adsorption tower with a distributor, which has the advantages of uniform adsorption and good adsorption effect.
  • Embodiments of the present invention also provide a flue gas purification system comprising the above-mentioned moving bed adsorption tower.
  • the moving bed adsorption tower includes a tower body, the tower body has a cavity, and the tower body is provided with a feeding port, a material outlet, a flue gas inlet and a flue gas outlet communicating with the cavity , the cavity has an inlet section, a packing section and an air outlet section in the flow direction of the flue gas, and the packing section is used to fill the adsorbent; the distributor, the distributor is arranged in the tower body, the distribution The distributor is provided with several feeding openings, and the distributor is located below the packing section so that the adsorbent in the packing section flows out through the feeding openings; a plurality of feeding pipes, a plurality of the feeding pipes and A plurality of the discharge openings correspond to each other, the discharge pipe is located below the discharge opening and there is a space between the discharge openings for the flow of smoke, and the smoke inlet is located at the discharge opening. Below the outlet, the drop tube is located above the outlet.
  • the moving bed adsorption tower according to the embodiment of the present invention has the advantages of uniform adsorption and good adsorption effect.
  • the distributor includes a distribution plate, the discharge opening is arranged on the distribution plate, the distribution plate is connected with the peripheral wall of the cavity, and the smoke inlet is located on the distribution plate below.
  • the vertical dimension of the gap between the top end of the drop tube and the lower end surface of the distribution plate is 20mm-100mm.
  • the discharge opening is a bar-shaped opening, a plurality of the discharge openings are arranged at intervals in the first direction, the discharge openings extend along the second direction, the first direction and the The second directions are perpendicular to each other.
  • the width of the discharge opening is 80mm-200mm
  • the size of the distributor in the second direction is L
  • the length of the discharge opening is 0.8L-0.95L.
  • the distance between two adjacent feeding openings is 100mm-300mm.
  • the distribution plate is rectangular, the length of the distribution plate is 1000mm-3000mm, the width of the distribution plate is 500mm-1500mm, the first direction is the length direction of the distribution plate, the The second direction is the width direction of the distribution plate.
  • the drop tube extends vertically, and the length of the drop tube in the vertical direction is 500mm-700mm.
  • the width of the opening at the upper end of the drop tube is greater than or equal to the radius of the accumulation corner of the adsorbent.
  • the drop tube includes a first section and a second section, the width of the first section is greater than the width of the second section, and the lower end of the first section is connected to the second section. connected at the top.
  • the width of the first section is 200mm-400mm, and the width of the second section is 100mm-200mm.
  • the flue gas inlet is located above the bottom end of the drop tube.
  • a flue gas cooling device the flue gas cooling device has a smoke inlet and a smoke outlet, and the flue gas cooling device is used to cool the flue gas entering from the smoke inlet to room temperature or below;
  • a moving bed adsorption tower is the moving bed adsorption tower described in any one of the above, the smoke outlet of the flue gas cooling device is connected with the flue gas outlet of the moving bed adsorption tower, the The moving bed adsorption tower is used to adsorb the flue gas.
  • FIG. 1 is a front view of a moving bed adsorption tower with a distributor according to an embodiment of the present invention
  • FIG. 2 is a top view of a moving bed adsorption tower with a distributor according to an embodiment of the present invention
  • Fig. 3 is the sectional view of A-A place among Fig. 2;
  • Fig. 4 is the sectional view of B-B place among Fig. 3;
  • Distributor 2 Distribution plate 21; Blanking port 22;
  • Falling pipe 3 first section 31; second section 32.
  • a moving bed adsorption tower with a distributor includes a tower body 1 , a distributor 2 and a plurality of downcomers 3 .
  • the tower body 1 is provided with a feed port 111, a discharge port 141, a flue gas inlet 131 and a flue gas outlet 121 communicating with the cavity, and the cavity has an inlet section in the flow direction of the flue gas 13.
  • the packing section 12 and the gas outlet section 11, the packing section 12 is used to fill the adsorbent;
  • the flue gas inlet 131 communicates with the air inlet section 13, the flue gas outlet 121 communicates with the gas outlet section 11, the feeding port 111 communicates with the gas outlet section 11, the feeding port 111 and the flue gas outlet 121 are located above the packing section 12, and the discharge The port 141 and the flue gas inlet 131 are located below the packing section 12 .
  • the flue gas flow direction is from the flue gas inlet 131 to the flue gas outlet 121 , and the gas outlet section 11 , packing section 12 and inlet section 13 are arranged sequentially from top to bottom.
  • the flue gas enters the interior of the tower body 1 from the lower half of the tower body 1 and flows out from the upper side of the tower body 1, and the adsorbent enters the tower body 1 from the upper side of the tower body 1 and flows out from the lower end of the tower body 1 , the flow direction of the flue gas is opposite to that of the adsorbent, the concentration of nitrogen and sulfur in the flue gas gradually decreases as the flue gas rises, the adsorption effect of the adsorbent gradually decreases with the contact time with the flue gas, and the lower nitrogen and sulfur concentrations
  • the flue gas is contacted with an adsorbent with good adsorption effect, which can effectively reduce the concentration of nitrogen and sulfur in the gas discharged from the flue gas outlet 121, and improve the adsorption efficiency.
  • the distributor 2 is arranged in the tower body 1, and the distributor 2 is provided with several blanking openings 22, and the distributor 2 is located below the packing section 12 so that the adsorbent in the packing section 12 flows out through the blanking openings 22;
  • the feeding openings 22 are through holes on the distributor 2, and the feeding openings 22 are arranged in parallel and at intervals with equal intervals.
  • the adsorbent enters the discharge pipe 3 through the discharge port 22, and the flow rate of the adsorbent through the uniformly arranged discharge ports 22 is approximately the same.
  • the contact time between the particles and the flue gas avoids the concentrated flow of the adsorbent from a position closer to the center of the tower body 1, resulting in dead angles in the flow, and improves the flow efficiency of the adsorbent, thereby improving the adsorption effect.
  • a plurality of blanking tubes 3 correspond to multiple blanking openings 22 one by one.
  • the blanking tubes 3 are located below the blanking openings 22 and there is a gap between them to facilitate the flow of flue gas.
  • the flue gas inlet 131 is located at the bottom of the blanking Below the mouth 22, the material drop pipe 3 is located above the material outlet 141.
  • the geometric center of the blanking opening 22 in the horizontal direction is the same as the geometric center of the blanking tube 3 in the horizontal direction, the upper end of the blanking tube 3 is spaced from the lower end of the distributor 2, and the smoke inlet 131 The upper edge is located below the blanking opening 22 to ensure that the flue gas inlet 131 is completely below the blanking opening 22 .
  • the flue gas enters the tower body 1 from the flue gas inlet 131, it enters the packing section 12 through the space between the blanking pipe 3 and the blanking port 22.
  • the path of the flue gas entering the seasoning section is shorter and smoother, and the smoke
  • the pressure drop caused by energy loss when the gas flows improves the fluency of the flue gas flowing in the packing section 12, thereby improving the adsorption effect.
  • the distributor 2 includes a distribution plate 21 on which the discharge opening 22 is arranged, the distribution plate 21 is connected to the peripheral wall of the cavity, and the smoke inlet 131 is located below the distribution plate 21 .
  • the distribution plate 21 is a perforated flat plate
  • the discharge opening 22 is a through hole on the distribution plate 21
  • the distribution plate 21 is arranged horizontally
  • the lower end of the distribution plate 21 is higher than the upper end of the flue gas inlet 131 . Therefore, the horizontal arrangement of the distribution plate 21 can ensure that the adsorbent is evenly distributed above the distribution plate 21, and ensure that the blanking is uniform to improve the efficiency of blanking.
  • the lower end of the distribution plate 21 is higher than the upper end of the flue gas inlet 131 so that all the smoke All the gas passes through the blanking port 22, which increases the contact time between the flue gas and the adsorbent particles, thereby improving the adsorption efficiency.
  • the vertical dimension of the gap between the top end of the drop tube 3 and the lower end surface of the distribution plate 21 is 20mm-100mm.
  • the vertical dimension of the gap between the discharge tube 3 and the distribution plate 21 can be any value between 20mm and 100mm.
  • the vertical dimension of the gap between the drop pipe 3 and the distribution plate 21 is 75 mm, so that the air passing through the gap reaches the required flow rate of the adsorption tower space velocity.
  • the discharge opening 22 is a bar-shaped opening, a plurality of discharge openings 22 are arranged at intervals in the first direction, the discharge opening 22 extends along the second direction, and the first direction and the second direction are perpendicular to each other.
  • the first direction is the left-right direction
  • the second direction is the front-rear direction
  • the blanking ports 22 are arranged at equal intervals along the first direction, thus, the blanking ports 22 are elongated.
  • the adsorbent particles can be completely dropped into the feeding pipe 3, and the cross-sectional area of the feeding opening 22 can be relatively large, so as to ensure the fluidity of the adsorbent particles.
  • the discharge opening 22 may be circular, triangular, rhombus and so on.
  • the width of the feeding opening 22 is 80mm-200mm
  • the size of the distributor 2 in the second direction is L
  • the length of the feeding opening 22 is 0.8L-0.95L.
  • the width of the blanking opening 22 can be any value between 80mm and 200mm, for example, the width of the blanking opening 22 can be 85mm, 100mm, 151.8mm, 200mm, etc.
  • the width of the material-feeding opening 22 is 290mm, so that the flow rate of the adsorbent particles flowing through the material-feeding opening 22 can meet the design requirement.
  • the width of the material opening 22 is the size of the material opening 22 in the first direction
  • the length of the material opening 22 is the size of the material opening 22 in the second direction.
  • the size of the distributor 2 in the second direction is 1850 mm, and the length of the discharge opening 22 is 900 mm, so that the flow rate of the adsorbent particles flowing through the discharge opening 22 meets the design requirements.
  • the distance between two adjacent feeding openings 22 is 100mm-300mm.
  • the interval between two adjacent blanking ports 22 is the distance between the two closest points in the first direction between two adjacent blanking ports 22, and the interval between two adjacent blanking ports 22 is It can be any value between 100mm and 300mm, for example, the interval between two adjacent discharge openings 22 can be 105mm, 159mm, 201.6mm, 300mm and so on.
  • the interval between two adjacent feeding openings 22 is 100mm, so that eight feeding openings 22 can be distributed on the distributor 2, so that the flow of adsorbent particles is more uniform.
  • the distribution plate 21 is rectangular, the length of the distribution plate 21 is 1000mm-3000mm, the width of the distribution plate 21 is 500mm-1500mm, the first direction is the length direction of the distribution plate 21, and the second direction is the direction of the distribution plate 21. the width direction.
  • the length of the distribution plate 21 is 2000mm, and the width of the distribution plate 21 is 1000mm, so that the distribution plate 21 can completely cover the cross section of the tower body 1, so that all the adsorbent particles flow downward through the distribution plate 21.
  • the distribution plate 21 may be circular, oval, triangular, etc.
  • the drop tube 3 extends vertically, and the length of the drop tube 3 in the vertical direction is 500mm-700mm.
  • the width of the opening at the upper end of the drop tube 3 is greater than or equal to the radius of the accumulation corner of the adsorbent.
  • the adsorbent particles will fall at the junction of the first section 31 and the second section 32, and accumulate in the first section 31 of the drop tube 3 to form a structure similar to a cone, and the radius of the accumulation angle refers to the above-mentioned
  • the radius of the cone the width of the upper opening of the drop tube 3 is the distance between the two ends of the drop tube 3 in the first direction.
  • the left and right walls of the drop tube 3 will not affect the accumulation of the adsorbent, reducing the impact of the shape of the drop tube 3 on the flow of the adsorbent particles through the drop tube 3, thereby preventing the adsorbent particles from flowing through the drop tube 3. leaked between.
  • the drop tube 3 includes a first section 31 and a second section 32, the width of the first section 31 is greater than that of the second section 32, and the lower end of the first section 31 is connected to the upper end of the second section 32.
  • the first section 31 of the drop tube 3 is located above the second section 32 of the drop tube 3, the cross section of the first section 31 of the drop tube 3 is elongated, and the cross section of the second section 32 of the drop tube 3 It is elongated, and the cross-sectional area of the second section 32 of the drop tube 3 is smaller than that of the first section 31 .
  • the larger cross-sectional area of the first section 31 is convenient for the adsorbent particles to fall into the first section 31, and the smaller cross-sectional area of the second section 32 is convenient for controlling the flow rate of the adsorbent particles flowing out of the discharge pipe 3 and the flow rate of the adsorbent particles into the discharge pipe. 3 with the same flow rate.
  • the width of the first section 31 is 200mm-400mm, and the width of the second section 32 is 100mm-200mm.
  • the width of the first section 31 and the second section 32 is the size of the first section 31 and the second section 32 along the first direction
  • the width of the first section 31 is the width of the opening at the upper end of the above-mentioned drop tube 3
  • the length of the first section 31 and the second section 32 is the size of the first section 31 and the second section 32 along the second direction
  • the length of the second section 32 can be equal to the first section 31, the length of the second section 32 It can also be shorter than the length of the first section 31 .
  • the width of the first segment 31 is greater than the width of the second segment 32 .
  • the width of the first section 31 is 290mm, and the width of the second section 32 is 100mm, so that the first section 31 can be sleeved on the lower end of the distribution pipe 22 .
  • the flue gas inlet 131 is located above the bottom end of the drop tube 3 .
  • the height of the lowermost end of the flue gas inlet 131 is higher than the height of the lower end of the discharge pipe 3 . Therefore, the flue gas inlet 131 is completely located above the lower end of the drop pipe 3, ensuring that when the adsorbent falls from the drop pipe 3, it will not splash out of the tower body 1 through the flue gas inlet 131, thereby improving the efficiency of adsorbent collection.
  • 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 communicates with the bottom of the discharge section 14 .
  • the cavity refers to the space inside the tower body 1
  • the discharge section 14 is an inverted quadrangular pyramid
  • the top of the discharge section 14 is connected with the inlet section 13
  • the discharge section 14 is a hollow structure
  • the inside of the discharge section 14 The space is connected with the cavity, the cross-sectional area of the discharge section 14 gradually decreases along the direction from top to bottom, and the discharge port 141 is arranged at the lower end of the discharge section 14 .
  • the adsorbent completes the adsorption of harmful components in the flue gas, it falls into the discharge section 14 through the discharge pipe 3 and is collected in the discharge section 14.
  • the material port 141 is discharged, and the recovered adsorbent is processed in the next step.
  • the material outlet 141 is closed, the harmful components escaping from the adsorbent flow upward together with the flue gas entering the flue gas inlet 131, and will not be volatilized. to the atmosphere.
  • the height of the discharge section 14 is 1.0m-3.0m. Specifically, the height of the discharge section 14 is the vertical distance between the top of the discharge section 14 and the bottom of the discharge section 14 .
  • the height of the discharge section 14 can be any value between 1.0m and 3.0m, for example, the height of the discharge section 14 can be 1.1m, 2.0m, 2.1m, 2.85m and so on.
  • the height of the discharge section 14 is 1.8m, so that the material flows downward smoothly.
  • the height of the moving bed adsorption tower is 4.0m-8.0m. Specifically, the height of the moving bed adsorption tower is the vertical distance between the feed port 111 and the discharge port 141 .
  • the height of the moving bed adsorption tower can be any value between 4.0m and 8.0m, for example, the height of the moving bed adsorption tower can be 4.1m, 5.02m, 6.15m, 7.8m, etc.
  • the height of the moving bed adsorption tower is 6.02m, which fully takes into account the height of the material layer and the space occupied.
  • the height of the inlet section 13 is 1.0m-2.0m
  • the height of the packing section 12 is 2.0m-3.0m
  • the height of the outlet section 11 is 0.5m-1m.
  • the height of the filler section 12 is greater than the sum of the inlet section 13 and the outlet section 11.
  • the height of the inlet section 13 is 1.5m
  • the height of the outlet section 11 is 0.6m
  • the height of the filler section 12 is 2.5m.
  • the height of the air inlet section 13 is 1.45m
  • the height of the filler section 12 is 2.05m
  • the height of the air outlet section 11 is 0.7m, so that the material can be covered with the distribution plate 21.
  • the space velocity of the moving bed adsorption tower is 600h -1 -1500h -1 .
  • 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.
  • the space velocity of the moving bed adsorption tower is 1000h -1 -1300h -1 , so that the moving bed adsorption tower has a preferable adsorption effect.
  • the flue gas purification system includes: a flue gas cooling device, the flue gas cooling device has a smoke inlet and a smoke outlet, and the flue gas cooling device is used to cool the flue gas entering from the smoke inlet to room temperature and Below: moving bed adsorption tower, the moving bed adsorption tower is the moving bed adsorption tower in any of the above-mentioned embodiments, the smoke outlet of the flue gas cooling device is communicated with the flue gas outlet 121 of the moving bed adsorption tower, and the moving bed adsorption tower is used for Adsorb the flue gas.
  • the temperature of the flue gas entering the flue gas inlet 131 is -100° C. to room temperature (for example, the room temperature is 25° C.).
  • the adsorbent is activated coke (carbon).
  • the flue gas purification system provided in this example adopts the low-temperature adsorption method when adsorbing the flue gas, and utilizes the dissolution characteristics and adsorption characteristics of the pollutant components in the flue gas at low temperatures to remove pollutants, and can simultaneously realize desulfurization and denitrification .
  • the sulfur dioxide in the flue gas is mainly physically adsorbed, the desorption temperature is low, the loss of the adsorbent is low, and the supplementary amount of the adsorbent is low, which reduces the operating cost.
  • the flue gas purification system that adsorbs at low temperature has a large adsorption capacity for pollutants, a small amount of adsorbent loading, and a small footprint for equipment such as moving bed adsorption towers.
  • the flue gas purification system provided in this example performs adsorption and purification of the flue gas
  • the NOx components that are difficult to remove in the flue gas are oxidized to NO2 by the mechanism of super-low temperature oxidation adsorption for adsorption and removal. It needs to inject NH3 for catalytic reduction, and the operation cost is low.
  • the flue gas purification system provided in this embodiment can absorb more than 99% of NO x in the flue gas, and the denitrification efficiency is obviously better than the 70-80% denitrification efficiency in the prior art.
  • first and second are used for descriptive purposes only, and cannot be interpreted as indicating or implying relative importance or implicitly specifying the quantity of indicated technical features.
  • the features defined as “first” and “second” may explicitly or implicitly include at least one of these features.
  • “plurality” means at least two, such as two, three, etc., unless otherwise specifically defined.
  • the first feature may be in direct contact with the first feature or the first and second feature may be in direct contact with the second feature through an intermediary. touch.
  • “above”, “above” and “above” the first feature on the second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature.
  • “Below”, “beneath” and “beneath” the first feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is less horizontally than the second feature.
  • the terms “one embodiment,” “some embodiments,” “example,” “specific examples,” or “some examples” mean specific features, structures, materials, or features described in connection with the embodiment or example.
  • a feature is included in at least one embodiment or example of the invention.
  • the schematic representations of the above terms are not necessarily directed to the same embodiment or example.
  • the described specific features, structures, materials or characteristics may be combined in any suitable manner in any one or more embodiments or examples.
  • those skilled in the art can combine and combine different embodiments or examples and features of different embodiments or examples described in this specification without conflicting with each other.

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Abstract

一种移动床吸附塔和烟气净化系统，包括塔体（1）、分布器（2）和多个落料管（3）。塔体（1）内具有空腔，塔体（1）设有与空腔连通的加料口（111）、出料口（141）、烟气进口（131）和烟气出口（121），空腔在烟气的流通方向上具有进气段（13）、填料段（12）和出气段（11），填料段（12）用于填充吸附剂；分布器（2）设在塔体（1）内，分布器（2）设有若干落料口（22），分布器（2）位于填料段（12）的下方以便填料段（12）中的吸附剂通过落料口（22）流出；多个落料管（3）与多个落料口（22）一一对应，落料管（3）位于落料口（22）的下方并与落料口（22）之间具有间隔以便烟气流动，烟气进口（131）位于落料口（22）的下方，落料管（3）位于出料口（141）的上方。该移动床吸附塔具有吸附均匀、吸附效果好的优点。

Description

具有分布器的移动床吸附塔和烟气净化系统
本申请要求以下中国专利发明的优先权，其全部内容通过引用结合在本申请中。(1)发明号：CN202111028517.8，发明日：2021年09月02日，申请人：中国华能集团有限公司，中国华能集团清洁能源技术研究院有限公司，发明创造名称：具有分布器的移动床吸附塔和烟气净化系统(2)发明号：202111082809.X，发明日：2021年09月15日，申请人：中国华能集团有限公司，中国华能集团清洁能源技术研究院有限公司，发明创造名称：具有分布器的移动床吸附塔和烟气净化系统。
技术领域
本申请涉及烟气处理技术领域，尤其是涉及一种具有分布器的移动床吸附塔和烟气净化系统。
背景技术
燃煤烟气产生大量的污染物是危害大气环境和人类健康的重要因素之一。烟气净化领域通常采用固定床吸附塔对烟气中的污染物进行吸附以实现净化烟气的目的，但是相关技术中的固定床吸附塔在应用时普遍存在填料层压力与密度不均匀、吸附不均匀、吸附效果差、吸附能力随使用时间延长而降低的问题，而且在需要更换吸附剂时需要停止工作，严重影响吸附效率，提高了操作难度。相关技术采用移动床吸附塔通过使吸附剂在塔内流动，克服了固定床吸附塔吸附能力随使用时间延长而降低的问题，但是移动床吸附塔中仍然存在烟 气分布不均匀、净化效果不理想的问题。
发明内容
本发明旨在至少在一定程度上解决相关技术中的技术问题之一。为此，本发明的实施例提出一种具有分布器的移动床吸附塔，具有吸附均匀、吸附效果好的优点。
本发明的实施例还提出一种包括上述移动床吸附塔的烟气净化系统。
根据本发明实施例的移动床吸附塔，包括塔体，所述塔体内具有空腔，所述塔体设有与所述空腔连通的加料口、出料口、烟气进口和烟气出口，所述空腔在烟气的流通方向上具有进气段、填料段和出气段，所述填料段用于填充吸附剂；分布器，所述分布器设在所述塔体内，所述分布器设有若干落料口，所述分布器位于所述填料段的下方以便所述填料段中的吸附剂通过所述落料口流出；多个落料管，多个所述落料管与多个所述落料口一一对应，所述落料管位于所述落料口的下方并与所述落料口之间具有间隔以便烟气流动，所述烟气进口位于所述落料口的下方，所述落料管位于所述出料口的上方。
根据本发明实施例的移动床吸附塔具有吸附均匀、吸附效果好的优点。
在一些实施例中，所述分布器包括分布板，所述落料口设在所述分布板上，所述分布板与所述空腔的周壁相连，所述烟气进口位于所述分布板的下方。
在一些实施例中，所述落料管的顶端与所述分布板的下端面之间的缝隙在竖直方向上的尺寸为20mm-100mm。
在一些实施例中，所述落料口为条形口，多个所述落料口在第一方向上间隔排布，所述落料口沿第二方向延伸，所述第一方向和所述第二方向相互垂直。
在一些实施例中，所述落料口的宽度为80mm-200mm，所述分布器在所述第二方向上的尺寸为L，所述落料口的长度的大小为0.8L-0.95L。
在一些实施例中，相邻两个落料口之间的间隔大小为100mm-300mm。
在一些实施例中，所述分布板为矩形，所述分布板的长度为1000mm-3000mm,所述分布板的宽度为500mm-1500mm，所述第一方向为所述分布板的长度方向，所述第二方向为所述分布板的宽度方向。
在一些实施例中，所述落料管沿竖直方向延伸，所述落料管在竖直方向上的长度为500mm-700mm。
在一些实施例中，所述落料管的上端开口的宽度大于等于所述吸附剂的堆积角的半径。
在一些实施例中，所述落料管包括第一段和第二段，所述第一段的宽度大于所述第二段的宽度，所述第一段的下端与所述第二段的上端相连。
在一些实施例中，所述第一段的宽度为200mm-400mm，所述第二段的宽度为100mm-200mm。
在一些实施例中，所述烟气进口位于所述落料管的底端的上方。
根据本发明实施例的烟气净化系统，包括：
烟气冷却装置，所述烟气冷却装置具有进烟口和出烟口，所述烟气冷却装置用于将从所述进烟口进入的烟气冷却至室温及以下；
移动床吸附塔，所述移动床吸附塔为上述任一项所述的移动床吸附塔，所述烟气冷却装置的出烟口与所述移动床吸附塔的所述烟气出口连通，所述移动床吸附塔用于对所述烟气进行吸附。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍。显而易见地，下面描述中的附图仅仅是本发明的一些示例或实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据提供的附图获得其他的附图，而且还可以根据提供的附图将本发明应用于其它类似情景。除非从语言环境中显而易见或另做说明，图中相同标号代表相同结构或操作。
图1是根据本发明实施例的具有分布器的移动床吸附塔的正视图；
图2是根据本发明实施例的具有分布器的移动床吸附塔的俯视图；
图3是图2中A-A处的剖视图；
图4是图3中B-B处的剖视图；
附图标记：
塔体1；出气段11；加料口111；填料段12；烟气出口121；进气段13；烟气进口131；出料段14；出料口141；
分布器2；分布板21；落料口22；
落料管3；第一段31；第二段32。
具体实施方式
下面结合附图和实施例对本发明作进一步的详细说明。可以理解的是，此处所描述的具体实施例仅仅用于解释相关发明，而非对该发明的限定。所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的 所有其他实施例，都属于本发明保护的范围。
如图1至图3所示，根据本发明实施例的具有分布器的移动床吸附塔，包括塔体1、分布器2和多个落料管3。
塔体1内具有空腔，塔体1设有与空腔连通的加料口111、出料口141、烟气进口131和烟气出口121，空腔在烟气的流通方向上具有进气段13、填料段12和出气段11，填料段12用于填充吸附剂；
具体地，烟气进口131与进气段13连通，烟气出口121与出气段11连通，加料口111与出气段11连通，加料口111和烟气出口121位于填料段12的上方，出料口141和烟气进口131位于填料段12的下方。需要说明的是，烟气流通方向是从烟气进口131到烟气出口121，出气段11、填料段12和进气段13沿着从上至下的方向依次排布。由此，烟气从塔体1的下半部进入塔体1的内部并从塔体1的上侧流出，吸附剂从塔体1的上侧进入塔体1并从塔体1的下端流出，烟气的流向与吸附剂的流向相反，烟气中氮和硫的浓度随着烟气上升逐渐降低，吸附剂的吸附效果随着与烟气接触的时间逐渐降低，较低氮和硫浓度的烟气较好吸附效果的吸附剂接触，能够有效降低从烟气出口121排出气体中氮和硫的浓度，提高吸附效率。
分布器2设在塔体1内，分布器2设有若干落料口22，分布器2位于填料段12的下方以便填料段12中的吸附剂通过落料口22流出；
具体地，落料口22是分布器2上的通孔，落料口22平行间隔布置且间距相等。由此，吸附剂穿过落料口22进入落料管3中，吸附剂通过均匀布置的各个落料口22的流量大致相同，一方面延缓了吸附剂向下流动的速度，增加了吸附剂颗粒与烟气接触的时间，另一方面避免吸附剂集中从更靠近塔体1 中心的位置流出、在流动中产生死角，提高了吸附剂流动的效率，从而提高了吸附效果。
多个落料管3与多个落料口22一一对应，落料管3位于落料口22的下方并与落料口22之间具有间隔以便烟气流动，烟气进口131位于落料口22的下方，落料管3位于出料口141的上方。
具体地，落料口22在水平方向上的几何中心与落料管3在水平方向上的几何中心的位置相同，落料管3的上端与分布器2的下端有间隔，烟气进口131的上沿位于落料口22的下方保证烟气进口131完全位于落料口22的下方。由此，烟气从烟气进口131进入塔体1后，经过落料管3与落料口22之间的间隔进入填料段12中，在烟气进入调料段的路径更短更平顺，烟气流动时由于能量损失而引起的压降低，提高了烟气在填料段12流动的流畅程度，从而提高了吸附效果。
在一些实施例中，分布器2包括分布板21，落料口22设在分布板21上，分布板21与空腔的周壁相连，烟气进口131位于分布板21的下方。
具体地，分布板21是多孔平板，落料口22即为分布板21上的通孔，分布板21水平布置，分布板21的下端高于烟气进口131的上端。由此，分布板21水平布置可以保证吸附剂均匀地分布在分布板21的上方，保证落料均匀从而提高落料的效率，分布板21的下端高于烟气进口131的上端可以使全部烟气都从落料口22中穿过，提高了烟气与吸附剂颗粒的接触时间，从而提高了吸附的效率。
在一些实施例中，落料管3的顶端与分布板21的下端面之间的缝隙在竖直方向上的尺寸为20mm-100mm。具体地，落料管3与分布板21之间的缝隙 在竖直方向上的尺寸可以为20mm至100mm之间的任意数值。
优选的，落料管3与分布板21之间的缝隙在竖直方向上的尺寸为75mm，这样设置使通过该缝隙的空气达到吸附塔空速所需的流量。
在一些实施例中，落料口22为条形口，多个落料口22在第一方向上间隔排布，落料口22沿第二方向延伸，第一方向和第二方向相互垂直。
具体地，如图4所示，第一方向即为左右方向，第二方向即为前后方向，落料口22沿着第一方向等间距布置，由此，落料口22为长条形既可以把吸附剂颗粒完全落入落料管3中，又可以保证较大的落料口22的截面积，从而保证吸附剂颗粒的流动性。
在其它一些实施例中，落料口22可以为圆形、三角形、菱形等。
在一些实施例中，落料口22的宽度为80mm-200mm，分布器2在第二方向上的尺寸为L，落料口22的长度的大小为0.8L-0.95L。
具体地，落料口22的宽度可以为80mm至200mm之间的任意数值，例如，落料口22的宽度可以为85mm、100mm、151.8mm、200mm等。优选的，落料口22的宽度为290mm，这样设置使吸附剂颗粒流经落料口22的流量达到设计要求。
需要说明的是，落料口22的宽度即为落料口22在第一方向上的尺寸，落料口22的长度即为落料口22在第二方向上的尺寸。
优选的，分布器2在第二方向上的尺寸为1850mm，落料口22的长度为900mm，这样设置使吸附剂颗粒流经落料口22的流量达到设计要求。
在一些实施例中，相邻两个落料口22之间的间隔大小为100mm-300mm。
具体地，相邻两个落料口22之间的间隔即为相邻两个落料口22在第一方 向上距离最近的两点的距离，相邻两个落料口22之间的间隔可以为100mm至300mm之间的任意数值，例如，相邻两个落料口22之间的间隔可以为105mm、159mm、201.6mm、300mm等。优选的，相邻两个落料口22之间的间隔为100mm，这样设置使分布器2上能够分布八个落料口22，从而使吸附剂颗粒流动更均匀。
在一些实施例中，分布板21为矩形，分布板21的长度为1000mm-3000mm,分布板21的宽度为500mm-1500mm，第一方向为分布板21的长度方向，第二方向为分布板21的宽度方向。优选的，分布板21的长度为2000mm，分布板21的宽度为1000mm，这样设置使分布板21能够完全覆盖塔体1的截面，使全部的吸附剂颗粒都经过分布板21向下流动。
在其他一些实施例中，分布板21可以为圆形、椭圆形、三角形等。
在一些实施例中，落料管3沿竖直方向延伸，落料管3在竖直方向上的长度为500mm-700mm。
在一些实施例中，落料管3的上端开口的宽度大于等于吸附剂的堆积角的半径。
具体地，吸附剂颗粒会掉落在第一段31和第二段32的连接处，在落料管3的第一段31堆积成类似于圆锥体的结构，堆积角的半径指的就是上述的圆锥体的半径，落料管3的上端开口的宽度即为落料管3在第一方向上两端之间的距离。由此，落料管3的左右两壁不会影响吸附剂的堆积，减少了落料管3外形对吸附剂颗粒穿过落料管3流量的影响，从而避免吸附剂颗粒从落料管3之间漏出。
在一些实施例中，落料管3包括第一段31和第二段32，第一段31的宽 度大于第二段32的宽度，第一段31的下端与第二段32的上端相连。
具体地，落料管3的第一段31位于落料管3第二段32的上方，落料管3的第一段31的截面是长条状，落料管3第二段32的截面是长条状，落料管3的第二段32的截面积小于第一段31。由此，第一段31的截面积较大便于吸附剂颗粒落入第一段31中，第二段32的截面积较小便于控制吸附剂颗粒流出落料管3的流速与流入落料管3的流速相同。
在一些实施例中，第一段31的宽度为200mm-400mm，第二段32的宽度为100mm-200mm。
具体地，第一段31和第二段32的宽度是第一段31和第二段32沿着第一方向的尺寸，第一段31的宽度即为上述的落料管3上端开口的宽度，第一段31和第二段32的长度是第一段31和第二段32沿着第二方向的尺寸，第二段32的长度可以与第一段31相等，第二段32的长度也可以小于第一段31的长度。第一段31的宽度大于第二段32的宽度。
优选的，第一段31的宽度为290mm，第二段32的宽度为100mm，这样设置使第一段31能够套在分布管22的下端。
在一些实施例中，烟气进口131位于落料管3的底端的上方。
具体地，烟气进口131的最下端的高度高于落料管3下端的高度。由此，烟气进口131完全位于落料管3下端的上方，保证吸附剂从落料管3中落下时，不会经过烟气进口131溅出塔体1，提高了吸附剂收集的效率。
在一些实施例中，空腔还包括位于出气段11下方的出料段14，出料段14呈倒锥型，出料口141与出料段14的底部连通。
具体地，空腔是指塔体1内部的空间，出料段14是倒四棱锥形，出料段 14的顶部与进气段13连接，出料段14是中空结构，出料段14内部的空间与空腔相连，出料段14的截面积沿着从上向下的方向逐渐减小，出料口141设置在出料段14的下端。由此，吸附剂在完成对烟气中有害成分的吸附后，经过落料管3落入出料段14，并在出料段14中进行收集，在收集一定数量的吸附剂后，从出料口141排出，对回收的吸附剂进行下一步的处理，在出料口141封闭时，吸附剂中逸出的有害成分与烟气进口131中进入的烟气一起向上流动，不会挥散到大气中。
在一些实施例中，出料段14的高度为1.0m-3.0m。具体地，出料段14的高度即为出料段14顶部与出料段14的底部在竖直方向上的距离。出料段14的高度可以为1.0m至3.0m之间的任意数值，例如，出料段14的高度可以为1.1m、2.0m、2.1m、2.85m等。
优选的，出料段14的高度为1.8m，这样设置使料向下流动顺畅。
在一些实施例中，移动床吸附塔的高度为4.0m-8.0m。具体地，移动床吸附塔的高度即为加料口111和出料口141在竖直方向上的距离。移动床吸附塔的高度可以为4.0m至8.0m之间的任意数值，例如，移动床吸附塔的高度可以为4.1m、5.02m、6.15m、7.8m等。
优选的，移动床吸附塔的高度为6.02m，这样设置充分考虑了料层高度以及空间占地。
在一些实施例中，进气段13的高度为1.0m-2.0m，填料段12的高度为2.0m-3.0m，出气段11的高度为0.5m-1m。
具体地，填料段12的高度大于进气段13与出气段11的和，例如进气段13的高度为1.5m，出气段11的高度为0.6m，填料段12的高度为2.5m，由此， 由于述填料段12的高度大于进气段13与出气段11的和，吸附剂在填料段12存留的时间大于在进气段13中与在出气段11中存留时间的和，增加了吸附剂对烟气进行吸附的时间，从而提高吸附效率。
优选的，进气段13的高度为1.45m，填料段12的高度为2.05m，出气段11的高度为0.7m，这样设置使料能布满布料板21。
在一些实施例中，移动床吸附塔的空速为600h -1-1500h -1。具体地，空速指的是移动床吸附塔的烟气流量与移动床吸附塔中吸附剂的装填体积之比。由此，移动床吸附塔的空速较高，在相同的烟气流量下移动床吸附塔的装填体积可以小于现有移动床吸附塔的装填体积，如此设置可以减小移动床吸附塔的体积，还可以减少塔内吸附剂的装填量。
优选地，移动床吸附塔的空速为1000h -1-1300h -1，使移动床吸附塔具有优选的吸附效果。
根据本发明实施例的烟气净化系统，包括：烟气冷却装置，烟气冷却装置具有进烟口和出烟口，烟气冷却装置用于将从进烟口进入的烟气冷却至室温及以下；移动床吸附塔，移动床吸附塔为上述任一实施例中的移动床吸附塔，烟气冷却装置的出烟口与移动床吸附塔的烟气出口121连通，移动床吸附塔用于对烟气进行吸附。
可选地，烟气进口131进入的烟气的温度为-100℃-室温(例如室温为25℃)。可选地，吸附剂为活性焦(碳)。
本实施例提供的烟气净化系统在对烟气进行吸附时采用低温吸附的方式，利用烟气中污染物组分在低温下的溶解特性和吸附特性进行污染物的脱出，能够同时实现脱硫脱硝。其中，烟气中的二氧化硫以物理吸附为主，解析温度低， 吸附剂损耗低，吸附剂补充量低，降低了运行成本。并且，在低温下进行吸附的烟气净化系统对污染物的吸附量大，吸附剂装填量少，移动床吸附塔等设备的占地面积小。
需要说明的是，本实施例提供的烟气净化系统在对烟气进行吸附净化时，烟气中难以脱除的NO x组分用过低温氧化吸附机理，氧化成NO 2吸附脱除，不需要喷入NH 3进行催化还原，运行成本低。本实施例提供的烟气净化系统对烟气中NO x的吸附比例大于99％，脱硝效率明显优于现有技术中70～80％的脱硝效率。
在本发明的描述中，需要理解的是，术语“中心”、“纵向”、“横向”、“长度”、“宽度”、“厚度”、“上”、“下”、“前”、“后”、“左”、“右”、“竖直”、“水平”、“顶”、“底”“内”、“外”、“顺时针”、“逆时针”、“轴向”、“径向”、“周向”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。
此外，术语“第一”、“第二”仅用于描述目的，而不能理解为指示或暗示相对重要性或者隐含指明所指示的技术特征的数量。由此，限定有“第一”、“第二”的特征可以明示或者隐含地包括至少一个该特征。在本发明的描述中，“多个”的含义是至少两个，例如两个，三个等，除非另有明确具体的限定。
在本发明中，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”、“固定”等术语应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或成一体；可以是机械连接，也可以是电连接或彼此可通讯；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通或两个元件的相互 作用关系，除非另有明确的限定。对于本领域的普通技术人员而言，可以根据具体情况理解上述术语在本发明中的具体含义。
在本发明中，除非另有明确的规定和限定，第一特征在第二特征“上”或“下”可以是第一和第二特征直接接触，或第一和第二特征通过中间媒介间接接触。而且，第一特征在第二特征“之上”、“上方”和“上面”可是第一特征在第二特征正上方或斜上方，或仅仅表示第一特征水平高度高于第二特征。第一特征在第二特征“之下”、“下方”和“下面”可以是第一特征在第二特征正下方或斜下方，或仅仅表示第一特征水平高度小于第二特征。
在本发明中，术语“一个实施例”、“一些实施例”、“示例”、“具体示例”、或“一些示例”等意指结合该实施例或示例描述的具体特征、结构、材料或者特点包含于本发明的至少一个实施例或示例中。在本说明书中，对上述术语的示意性表述不必须针对的是相同的实施例或示例。而且，描述的具体特征、结构、材料或者特点可以在任一个或多个实施例或示例中以合适的方式结合。此外，在不相互矛盾的情况下，本领域的技术人员可以将本说明书中描述的不同实施例或示例以及不同实施例或示例的特征进行结合和组合。
尽管上面已经示出和描述了本发明的实施例，可以理解的是，上述实施例是示例性的，不能理解为对本发明的限制，本领域的普通技术人员在本发明的范围内可以对上述实施例进行变化、修改、替换和变型。

Claims (13)

  1. 一种具有分布器的移动床吸附塔，其特征在于，包括：
    塔体，所述塔体内具有空腔，所述塔体设有与所述空腔连通的加料口、出料口、烟气进口和烟气出口，所述空腔在烟气的流通方向上具有进气段、填料段和出气段，所述填料段用于填充吸附剂；
    分布器，所述分布器设在所述塔体内，所述分布器设有若干落料口，所述分布器位于所述填料段的下方以便所述填料段中的吸附剂通过所述落料口流出；
    多个落料管，多个所述落料管与多个所述落料口一一对应，所述落料管位于所述落料口的下方并与所述落料口之间具有间隔以便烟气流动，所述烟气进口位于所述落料口的下方，所述落料管位于所述出料口的上方。
  2. 根据权利要求1所述的具有分布器的移动床吸附塔，其特征在于，所述分布器包括分布板，所述落料口设在所述分布板上，所述分布板与所述空腔的周壁相连，所述烟气进口位于所述分布板的下方。
  3. 根据权利要求2所述的具有分布器的移动床吸附塔，其特征在于，所述落料管的顶端与所述分布板的下端面之间的缝隙在竖直方向上的尺寸为20mm-100mm。
  4. 根据权利要求1-3中任一项所述的具有分布器的移动床吸附塔，其特征在于，所述落料口为条形口，多个所述落料口在第一方向上间隔排布，所述落料口沿第二方向延伸，所述第一方向和所述第二方向相互垂直。
  5. 根据权利要求4所述的具有分布器的移动床吸附塔，其特征在于，所述落料口的宽度为80mm-200mm，所述分布器在所述第二方向上的尺寸为L， 所述落料口的长度的大小为0.8L-0.95L。
  6. 根据权利要求5所述的具有分布器的移动床吸附塔，其特征在于，相邻两个落料口之间的间隔大小为100mm-300mm。
  7. 根据权利要求4所述的具有分布器的移动床吸附塔，其特征在于，所述分布板为矩形，所述分布板的长度为1000mm-3000mm,所述分布板的宽度为500mm-1500mm，所述第一方向为所述分布板的长度方向，所述第二方向为所述分布板的宽度方向。
  8. 根据权利要求1所述的具有分布器的移动床吸附塔，其特征在于，所述落料管沿竖直方向延伸，所述落料管在竖直方向上的长度为500mm-700mm。
  9. 根据权利要求1或8所述的具有分布器的移动床吸附塔，其特征在于，所述落料管的上端开口的宽度大于等于所述吸附剂的堆积角的半径。
  10. 根据权利要求9所述的具有分布器的移动床吸附塔，其特征在于，所述落料管包括第一段和第二段，所述第一段的宽度大于所述第二段的宽度，所述第一段的下端与所述第二段的上端相连。
  11. 根据权利要求10所述的具有分布器的移动床吸附塔，其特征在于，所述第一段的宽度为200mm-400mm，所述第二段的宽度为100mm-200mm。
  12. 根据权利要求1所述的具有分布器的移动床吸附塔，其特征在于，所述烟气进口位于所述落料管的底端的上方。
  13. 一种烟气净化系统，其特征在于，包括：
    烟气冷却装置，所述烟气冷却装置具有进烟口和出烟口，所述烟气冷却装置用于将从所述进烟口进入的烟气冷却至室温及以下；
    移动床吸附塔，所述移动床吸附塔为根据权利要求1-12中任一项所述的 具有分布器的移动床吸附塔，所述烟气冷却装置的出烟口与所述移动床吸附塔的所述烟气出口连通，所述具有分布器的移动床吸附塔用于对所述烟气进行吸附。
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Publication number Priority date Publication date Assignee Title
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Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3732567A1 (de) * 1987-05-07 1988-11-24 Horst Dr Grochowski Anstroemboden fuer wanderbettreaktoren sowie verfahren zum betreiben dieser vorrichtung
US5441704A (en) * 1989-05-19 1995-08-15 Grochowski; Horst Fluidized bed reactor arrangement
WO1996024432A1 (en) * 1995-02-10 1996-08-15 Kovinska Industrija Vransko Flue gas purification apparatus
CN107661681A (zh) * 2017-11-08 2018-02-06 中国科学院过程工程研究所 一种烟气污染物净化塔
CN111841240A (zh) * 2019-04-26 2020-10-30 英特佳工程与环境技术有限公司 向吸附剂和/或吸收剂中装载氨气的容器和方法
CN113797712A (zh) * 2021-09-02 2021-12-17 中国华能集团有限公司 烟气净化系统和移动床吸附塔
CN113797710A (zh) * 2021-09-02 2021-12-17 中国华能集团有限公司 烟气净化系统及其移动床吸附塔
CN113828112A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 移动床吸附塔和具有移动床吸附塔的烟气净化系统
CN113828111A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 具有分布器的移动床吸附塔和烟气净化系统
CN113828110A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 移动床吸附塔和具有其的烟气净化系统
CN113828108A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 烟气净化系统、移动床吸附塔
CN113828109A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 烟气净化系统及其具有分布器的移动床吸附塔

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103230723B (zh) * 2013-04-22 2015-01-07 西安西热锅炉环保工程有限公司 一种圆环形分段式错流烟气净化吸附塔
CN113144825A (zh) * 2021-06-06 2021-07-23 国电环境保护研究院有限公司 一种工业尾气处理多循环吸附塔

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3732567A1 (de) * 1987-05-07 1988-11-24 Horst Dr Grochowski Anstroemboden fuer wanderbettreaktoren sowie verfahren zum betreiben dieser vorrichtung
US5441704A (en) * 1989-05-19 1995-08-15 Grochowski; Horst Fluidized bed reactor arrangement
WO1996024432A1 (en) * 1995-02-10 1996-08-15 Kovinska Industrija Vransko Flue gas purification apparatus
CN107661681A (zh) * 2017-11-08 2018-02-06 中国科学院过程工程研究所 一种烟气污染物净化塔
CN111841240A (zh) * 2019-04-26 2020-10-30 英特佳工程与环境技术有限公司 向吸附剂和/或吸收剂中装载氨气的容器和方法
CN113797712A (zh) * 2021-09-02 2021-12-17 中国华能集团有限公司 烟气净化系统和移动床吸附塔
CN113797710A (zh) * 2021-09-02 2021-12-17 中国华能集团有限公司 烟气净化系统及其移动床吸附塔
CN113828112A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 移动床吸附塔和具有移动床吸附塔的烟气净化系统
CN113828111A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 具有分布器的移动床吸附塔和烟气净化系统
CN113828110A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 移动床吸附塔和具有其的烟气净化系统
CN113828108A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 烟气净化系统、移动床吸附塔
CN113828109A (zh) * 2021-09-02 2021-12-24 中国华能集团有限公司 烟气净化系统及其具有分布器的移动床吸附塔

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