CN110585912A - Desulfurization and denitrification tower with desulfurization and denitrification catalyst beds arranged in staggered mode - Google Patents

Desulfurization and denitrification tower with desulfurization and denitrification catalyst beds arranged in staggered mode Download PDF

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Publication number
CN110585912A
CN110585912A CN201910932603.8A CN201910932603A CN110585912A CN 110585912 A CN110585912 A CN 110585912A CN 201910932603 A CN201910932603 A CN 201910932603A CN 110585912 A CN110585912 A CN 110585912A
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China
Prior art keywords
desulfurization
denitrification
catalyst bed
tower
catalyst
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CN201910932603.8A
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Inventor
杨颖欣
钟璐
胡静龄
刘勇
胡小吐
杨森林
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Guangdong Jiade Environmental Protection Technology Co Ltd
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Guangdong Jiade Environmental Protection Technology Co Ltd
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Priority to CN201910932603.8A priority Critical patent/CN110585912A/en
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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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B01D53/1481—Removing sulfur dioxide or sulfur trioxide
    • 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
    • B01D53/14—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 absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8609—Sulfur oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/869—Multiple step processes
    • 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

Abstract

The invention provides a desulfurization and denitrification tower with staggered desulfurization and denitrification catalyst beds, wherein a desulfurization catalyst bed and a denitrification catalyst bed are arranged in a tower body at intervals, the desulfurization catalyst bed is an unsaturated polyester resin matrix-loaded desulfurization catalyst, and the denitrification catalyst bed is an unsaturated polyester resin matrix-loaded denitrification catalyst. The desulfurization and denitrification tower combines the desulfurization step and the denitrification step, so that the occupied areas of the desulfurization tower and the denitrification tower are reduced, and the desulfurization and denitrification efficiency and the desulfurization and denitrification effect are improved.

Description

Desulfurization and denitrification tower with desulfurization and denitrification catalyst beds arranged in staggered mode
Technical Field
The invention belongs to the field of waste gas treatment, relates to a desulfurization and denitrification tower, and particularly relates to a desulfurization and denitrification tower with staggered desulfurization and denitrification catalyst beds.
Background
The coke oven flue waste gas is a product after combustion of a coke oven heating system, the temperature is below 300 ℃, the temperature at the root of a chimney is about 230-280 ℃, and the waste gas contains a large amount of heat energy and is recycled. Meanwhile, NO harmful to the environment is generated in a high-temperature state in the combustion process of the coke oven heating fuelxNO in the exhaust gas depending on the fuel used for heating the coke ovenxAlso varies, but usually NO is present in the exhaust gasxThe concentration of (A) exceeds the emission limit value regulated by the relevant national standard, and NO in flue gas is required to be treatedxAnd (4) carrying out removal, namely denitration treatment.
For flue gas with lower temperature, the most common method for flue gas denitration is an SCR (selective catalytic reduction) method. In the SCR process, a reducing agent reacts NO under the action of a catalystxReduced to nitrogen and water, catalyst for promoting reductant and NOxThe reducing agent is mainly ammonia, and can realize better denitration effect generally at more than 300 ℃, so that a smoke heating device needs to be additionally arranged for smoke lower than 300 ℃. In the prior coke oven flue gas denitration practice, an SCR method is adopted, liquid ammonia is used as a reducing agent, and in order to ensure the denitration effect, a gas heating furnace is additionally arranged to heat flue gas. Therefore, besides the SCR reaction device, an ammonia station, a flue gas heating system, a boiler waste heat recovery system, and a GGH heat exchange device need to be constructed in a matching manner, which results in a huge whole system, high investment, and high energy consumption.
In the existing desulfurization and denitrification processes, the desulfurization process and the denitrification process are respectively carried out in a desulfurization tower and a denitrification tower, so that the occupied area is large, the denitrification process or some magazine products generated after the desulfurization process can generate toxic effect on the catalyst in subsequent operation, the service life of the catalyst is shortened, and the cost of the desulfurization and denitrification process is increased, so that a new desulfurization and denitrification device needs to be developed.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a desulfurization and denitrification tower, which combines a desulfurization step and a denitrification step, reduces the occupied areas of the desulfurization tower and the denitrification tower, and improves the desulfurization and denitrification efficiency and the desulfurization and denitrification effect.
In order to achieve the purpose, the invention adopts the following technical scheme:
one purpose of the invention is to provide a desulfurization catalyst bed layer and a denitration catalyst bed layer which are arranged at intervals in the tower body, wherein the desulfurization catalyst bed layer is an unsaturated polyester resin matrix supported desulfurization catalyst, and the denitration catalyst bed layer is an unsaturated polyester resin matrix supported denitration catalyst.
In the invention, the desulfurization catalyst bed layer and the denitration catalyst bed layer are arranged at intervals, so that the gas composition in the flue gas can be changed after the flue gas passes through the desulfurization catalyst and the denitration catalyst, the partial pressure of each gas can be changed, and in the same tower body, if the flue gas is subjected to desulfurization after complete denitration or is subjected to denitration after complete desulfurization, the partial pressure of the gas in the flue gas can be greatly changed, so that the partial pressure of sulfur-containing compounds or nitrogen-containing compounds is greatly changed, and the subsequent removal and the stability of the desulfurization and denitration tower are not facilitated. And the interval sets up, can be so that for the gas partial pressure become the gradient and change, reduce the influence of partial pressure change to SOx/NOx control, be favorable to the stability of production.
As the preferable technical scheme of the invention, the bottom of the desulfurization and denitrification tower is provided with an air inlet, and the top of the desulfurization and denitrification tower is provided with an air outlet.
As a preferable technical scheme of the invention, an air inlet of the desulfurization and denitrification tower is connected with a dust removal device.
In the invention, because the desulfurization catalyst bed layer and the denitration catalyst bed layer are of porous structures, dust removal treatment needs to be carried out before flue gas enters the desulfurization and denitration tower provided by the invention, so that the catalyst bed layer is prevented from being blocked by impurities such as smoke dust and the like, and the desulfurization and denitration of the desulfurization and denitration tower are reduced.
As a preferable technical scheme of the invention, the gas outlet of the desulfurization and denitrification tower is connected with the absorption tower.
In the invention, the desulfurization catalyst bed layer and the denitration catalyst bed layer can be loaded with any one of desulfurization catalyst and denitration catalyst, and when the desulfurization catalyst is catalytic oxidation SO2At this time, SO2Conversion to SO3An absorption tower or other absorption devices are required to be arranged behind the desulfurization and denitrification tower to absorb the generated SO3。
In a preferred embodiment of the present invention, the height of the desulfurization and denitrification tower is 5 to 10m, such as 6m, 6.5m, 7m, 7.5m, 8m, 8.5m, 9m or 9.5m, but the tower is not limited to the above-mentioned values, and other values not listed in the above-mentioned value range are also applicable.
As a preferable technical scheme of the invention, the number of the desulfurization catalyst bed layers and the denitration catalyst bed layers is respectively and independently 2-5.
In the invention, the number of the desulfurization catalyst bed layer and the denitration catalyst bed layer can be determined according to SO in the flue gas2And NOXThe amount of the desulfurization catalyst bed layers and the amount of the denitration catalyst bed layers can be equal or unequal, but the alternate arrangement is ensured.
In a preferred embodiment of the present invention, the distance between the adjacent desulfurization catalyst beds and the adjacent denitration catalyst beds is 0.2 to 0.8m, such as 0.3m, 0.4m, 0.5m, 0.6m, or 0.7m, but is not limited to the above-mentioned values, and other values not listed in the above-mentioned range are also applicable.
In the invention, although the desulfurization catalyst bed layers and the denitration catalyst bed layers are limited to be arranged at intervals, the distance between the adjacent desulfurization catalyst bed layers and the adjacent denitration catalyst bed layers is not required to be equal, namely, the beds are not required to be arranged at equal intervals, and the distance between the adjacent catalyst bed layers can be adjusted according to the design value of simulation calculation or the actual application condition.
As a preferable technical scheme of the invention, the unsaturated polyester resin is a copolymer of maleic anhydride and 1, 2-propylene glycol.
Preferably, the unsaturated polyester resin has a weight average molecular weight of 1000 to 2000, such as 1100, 1200, 1500, 1600, 1800, and the like, but is not limited to the recited values, and other values not recited within the range of values are equally applicable.
In the present invention, the selection of the unsaturated polyester resin is not limited to the above-listed resins, the polymerization monomer and the unsaturation degree thereof can be selected according to the actual catalytic requirements, the polymerization degree thereof should be selected according to the porosity of the catalyst bed, too high polymerization degree can result in too high viscosity of the unsaturated polyester resin and reduced porosity of the catalyst bed, while too low polymerization degree can make the formation of the unsaturated polyester resin difficult, which is not beneficial to the preparation of the device.
In a preferred embodiment of the present invention, the mass fraction of the desulfurization catalyst in the desulfurization catalyst bed is 2 to 5%, for example, 2.5%, 3%, 3.5%, 4%, or 4.5%, but not limited to the recited values, and other values not recited in the above range are also applicable.
Preferably, the mass fraction of the denitration catalyst in the denitration catalyst bed is 1.5-2.5%, such as 1.6%, 1.7%, 1.8%, 1.9%, 2.0%, 2.1%, 2.2%, 2.3%, or 2.4%, but not limited to the recited values, and other non-recited values in the range of the values are also applicable.
In a preferred embodiment of the present invention, the desulfurization catalyst bed has a porosity of 15 to 30%, for example, 16%, 18%, 20%, 22%, 25%, or 28%, but the porosity is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are also applicable.
Preferably, the denitration catalyst bed has a porosity of 15 to 30%, such as 16%, 18%, 20%, 22%, 25%, or 28%, but not limited to the recited values, and other values not recited in the range of values are also applicable.
In the inventionThe method adopts a catalyst bed layer loaded by unsaturated polyester resin to respectively load a desulfurization catalyst and a denitration catalyst, and the catalyst bed layers are arranged in a staggered manner in the same tower body. Unsaturated polyester resin is adopted to load a desulfurization catalyst and a denitration catalyst, SO that unsaturated bonds can generate free radicals under the action of the catalyst at a certain temperature, and the free radicals can cooperate with the desulfurization or denitration catalyst to treat SO in flue gas2And NOXAnd removing. Because the catalyst evenly distributed in unsaturated polyester resin, can reduce the influence of the impurity that produces in desulfurization and denitration reaction to desulfurization catalyst and denitration catalyst for desulfurization catalyst and denitration catalyst can merge in same tower body, have reduced the area occupied of equipment. The staggered arrangement of the desulfurization catalyst bed layer and the denitration catalyst bed layer can ensure that SO in the flue gas2And NOXThe composition gradient is reduced, which is beneficial to the desulfurization and denitrification reaction.
Compared with the prior art, the invention at least has the following beneficial effects:
the invention provides a desulfurization and denitrification tower, which combines a desulfurization step and a denitrification step, reduces the occupied areas of the desulfurization tower and the denitrification tower, and improves the desulfurization and denitrification efficiency and the desulfurization and denitrification effect.
Drawings
FIG. 1 is a schematic view of the structure of a desulfurization and denitrification tower used in example 1;
FIG. 2 is a schematic view showing the structure of a desulfurization and denitrification tower used in example 2;
FIG. 3 is a schematic view of the structure of a desulfurization and denitrification tower used in example 3;
FIG. 4 is a schematic view of the structure of a desulfurization and denitrification tower used in example 4;
in the figure: the method comprises the following steps of 1-a desulfurization and denitrification tower main body, 2-a denitrification catalyst bed layer, 3-a desulfurization catalyst bed layer, 4-an air inlet and 5-an air inlet.
The present invention is described in further detail below. The following examples are merely illustrative of the present invention and do not represent or limit the scope of the claims, which are defined by the claims.
Detailed Description
The technical scheme of the invention is further explained by the specific implementation mode in combination with the attached drawings.
To better illustrate the invention and to facilitate the understanding of the technical solutions thereof, typical but non-limiting examples of the invention are as follows:
example 1
The embodiment provides a desulfurization and denitrification tower with staggered desulfurization and denitrification catalyst beds, which has a structure shown in fig. 1, wherein a desulfurization catalyst bed and a denitrification catalyst bed are arranged inside the tower body at intervals, the desulfurization catalyst bed is an unsaturated polyester resin matrix-loaded desulfurization catalyst, and the denitrification catalyst bed is an unsaturated polyester resin matrix-loaded denitrification catalyst.
The height of the desulfurization and denitrification tower is 5m, the interval between two adjacent catalysts and beds is 0.2m, the number of the desulfurization catalyst beds and the number of the denitrification catalyst beds are 4 respectively, the mass fraction of the desulfurization catalyst in the desulfurization catalyst beds is 2%, the mass fraction of the denitrification catalyst in the denitrification catalyst beds is 1.5%, and the porosity of the desulfurization catalyst beds and the porosity of the denitrification catalyst beds are 15%.
Example 2
The embodiment provides a desulfurization and denitrification tower with staggered desulfurization and denitrification catalyst beds, which has a structure shown in fig. 2, wherein a desulfurization catalyst bed and a denitrification catalyst bed are arranged inside the tower body at intervals, the desulfurization catalyst bed is an unsaturated polyester resin matrix-loaded desulfurization catalyst, and the denitrification catalyst bed is an unsaturated polyester resin matrix-loaded denitrification catalyst.
The height of the desulfurization and denitrification tower is 10m, the interval between two adjacent catalysts and beds is 0.8m, each of the number of the desulfurization catalyst bed layers and the number of the denitrification catalyst bed layers are 5, the mass fraction of the desulfurization catalyst in the desulfurization catalyst bed layers is 5%, the mass fraction of the denitrification catalyst in the denitrification catalyst bed layers is 2.5%, and the porosity of the desulfurization catalyst bed layers and the porosity of the denitrification catalyst bed layers are both 30%.
Example 3
The embodiment provides a desulfurization and denitrification tower with staggered desulfurization and denitrification catalyst beds, which has a structure shown in fig. 3, wherein a desulfurization catalyst bed and a denitrification catalyst bed are arranged inside the tower body at intervals, the desulfurization catalyst bed is an unsaturated polyester resin matrix-loaded desulfurization catalyst, and the denitrification catalyst bed is an unsaturated polyester resin matrix-loaded denitrification catalyst.
The height of the desulfurization and denitrification tower is 8m, the interval between two adjacent catalysts and beds is 0.6m, the number of the desulfurization catalyst beds and the number of the denitrification catalyst beds are 3 respectively, the mass fraction of the desulfurization catalyst in the desulfurization catalyst beds is 3%, the mass fraction of the denitrification catalyst in the denitrification catalyst beds is 1.8%, and the porosity of the desulfurization catalyst beds and the porosity of the denitrification catalyst beds are both 20%.
Example 4
The embodiment provides a desulfurization and denitrification tower with staggered desulfurization and denitrification catalyst beds, which has a structure shown in fig. 4, wherein a desulfurization catalyst bed and a denitrification catalyst bed are arranged inside the tower body at intervals, the desulfurization catalyst bed is an unsaturated polyester resin matrix-loaded desulfurization catalyst, and the denitrification catalyst bed is an unsaturated polyester resin matrix-loaded denitrification catalyst.
The height of the desulfurization and denitrification tower is 6m, the interval between two adjacent catalysts and beds is 0.8m, each of the number of the desulfurization catalyst bed layers and the number of the denitrification catalyst bed layers are 2, the mass fraction of the desulfurization catalyst in the desulfurization catalyst bed layers is 2.5%, the mass fraction of the denitrification catalyst in the denitrification catalyst bed layers is 2%, and the porosity of the desulfurization catalyst bed layers and the porosity of the denitrification catalyst bed layers are 25%.
Comparative example 1
The conditions in this comparative example were the same as those in example 1 except that two denitration and desulfurization towers each having 4 catalyst bed layers connected in series were used.
Comparative example 2
The conditions in this comparative example were the same as those in example 2 except that two denitration and desulfurization towers each having 5 catalyst bed layers connected in series were used.
Comparative example 3
The conditions in this comparative example were the same as those in example 3 except that the denitration tower and the desulfurization tower were used in which the number of catalyst bed layers was 3 in each case.
Comparative example 4
The conditions in this comparative example were the same as those in example 4 except that two denitration and desulfurization towers each having 2 catalyst bed layers connected in series were used.
In a specific embodiment of the present invention, the methods for preparing the desulfurization catalyst bed and the denitration catalyst bed used in examples 1 to 4 and comparative examples 1 to 4 are as follows:
mixing maleic anhydride and 1, 2-propylene glycol according to a molar ratio of 1:1.05, adding cumene hydroperoxide accounting for 0.01% of the total mass of the raw materials as an initiator, adding a desulfurization catalyst or a denitration catalyst according to a corresponding mass fraction, heating at 160 ℃ for 0.5h under the protection of nitrogen until refluxing, heating to 200 ℃ at a speed of 4 ℃/min, preserving heat for 6h, pouring a product into a mold after the reaction is finished, and naturally cooling to room temperature to obtain a corresponding catalyst bed layer.
In a specific embodiment of the present invention, the desulfurization catalyst and the denitration catalyst used in examples 1 to 4 and comparative examples 1 to 4 are vanadium pentoxide and coke, respectively.
The desulfurization and denitrification tower or the desulfurization and denitrification device provided in examples 1 to 4 and comparative examples 1 to 4 was used to treat flue gas, which was dedusted by a dedusting device and then flowed at 25000Nm3The concentration of sulfur oxides in the flue gas is 1200mg/Nm3The concentration of nitrogen oxides is 280mg/Nm3The temperature of the flue gas is 250 ℃. After passing through the desulfurization and denitrification device, the flue gas enters an absorption device using water as an absorption medium, and the dried treated flue gas is tested to obtain the desulfurization rate and the denitrification rate, and the results are shown in table 1.
TABLE 1
As can be seen from the test results in table 1, in examples 1 to 4, compared with corresponding comparative examples 1 to 4, the desulfurization and denitrification tower using the desulfurization catalyst bed layer and the denitrification catalyst bed layer arranged at intervals has a higher desulfurization rate and a higher denitrification rate than the desulfurization and denitrification device in which the corresponding denitrification tower and the desulfurization tower are connected in series. As can be seen from the comparison of the desulfurization rates and the denitration rates in examples 1 to 4, the difference between the numbers of the desulfurization catalyst beds and the denitration catalyst beds of 4 and 5 is small, that is, the numbers of the desulfurization catalyst beds and the denitration catalyst beds in the column do not need to be increased.
The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above embodiments, but the present invention is not limited to the above detailed structural features, that is, it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be understood by those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, additions of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.

Claims (10)

1. The utility model provides a desulfurization denitration tower that desulfurization denitration catalyst bed staggered arrangement which characterized in that, tower body inside interval is provided with desulfurization catalyst bed and denitration catalyst bed, desulfurization catalyst bed is unsaturated polyester resin base member load desulfurization catalyst, denitration catalyst bed is unsaturated polyester resin base member load denitration catalyst.
2. The desulfurization and denitrification tower of claim 1, wherein the desulfurization and denitrification tower is provided with a gas inlet at the bottom and a gas outlet at the top.
3. The desulfurization and denitrification tower of claim 1 or 2, wherein the gas inlet of the desulfurization and denitrification tower is connected with a dust removal device.
4. The desulfurization and denitrification tower according to any one of claims 1-3, wherein the outlet of the desulfurization and denitrification tower is connected with an absorption tower.
5. The desulfurization and denitrification tower according to any one of claims 1 to 4, wherein the height of the desulfurization and denitrification tower is 5-10 m.
6. The desulfurization and denitrification tower according to any one of claims 1 to 5, wherein the number of the desulfurization catalyst bed layers and the number of the denitrification catalyst bed layers are respectively and independently 2 to 5.
7. The desulfurization and denitrification tower according to any one of claims 1 to 6, wherein the interval between adjacent desulfurization catalyst beds and denitrification catalyst beds is 0.2-0.8 m.
8. The desulfurization and denitrification tower of any one of claims 1-7, wherein the unsaturated polyester resin is a copolymer of maleic anhydride and 1, 2-propylene glycol;
preferably, the unsaturated polyester resin has a weight average molecular weight of 1000 to 2000.
9. The desulfurization and denitrification tower according to any one of claims 1-8, wherein the mass fraction of the desulfurization catalyst in the desulfurization catalyst bed layer is 2-5%;
preferably, the mass fraction of the denitration catalyst in the denitration catalyst bed layer is 1.5-2.5%.
10. The desulfurization and denitrification tower according to any one of claims 1-8, wherein the desulfurization catalyst bed has a porosity of 15-30%;
preferably, the porosity of the denitration catalyst bed layer is 15-30%.
CN201910932603.8A 2019-09-29 2019-09-29 Desulfurization and denitrification tower with desulfurization and denitrification catalyst beds arranged in staggered mode Pending CN110585912A (en)

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