CN219463017U - Device for low-temperature denitration and desulfurization of flue gas and VOC removal - Google Patents
Device for low-temperature denitration and desulfurization of flue gas and VOC removal Download PDFInfo
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- CN219463017U CN219463017U CN202320412772.0U CN202320412772U CN219463017U CN 219463017 U CN219463017 U CN 219463017U CN 202320412772 U CN202320412772 U CN 202320412772U CN 219463017 U CN219463017 U CN 219463017U
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Abstract
The utility model discloses a device for low-temperature denitration, desulfurization and VOC removal of flue gas, which comprises an adsorption bin, wherein porous adsorption media are filled in the adsorption bin, and the flue gas directionally flows through the adsorption bin in the direction of flowing through the porous adsorption media; and a desorption bin in intermittent communication with the adsorption bin, from which the porous adsorption medium can flow into the desorption bin; the desorption bin has the characteristic of heating the porous adsorption medium, and is also provided with a desorption outlet. The utility model realizes low-temperature denitration and desulfurization, removes VOC, is not influenced by the temperature of waste gas, and can be operated at normal temperature.
Description
Technical Field
The utility model belongs to the technical field of waste gas treatment, and particularly relates to a device for low-temperature denitration, desulfurization and VOC removal of flue gas.
Background
The denitration and desulfurization VOC removal technology is a just-needed link in the industries of global thermal power, building materials, coking, chemical industry, garbage incineration and power generation, biomass power generation and the like, and a Selective Catalytic Reduction (SCR) denitration and desulfurization technology and a catalytic oxidation combustion method (RCO) -VOC removal technology are used in large quantities as a main flow technology in the industrial fields, and if 3 pollutants need to be treated simultaneously, the two technologies need to be used in series, so that the investment and the energy consumption are large.
The total pollutant emission amount is reduced by adopting measures such as load reduction in industry, so that the gas amount and the temperature of the flue gas (industrial waste gas) fluctuate in a wider interval, the poisoning failure of a catalyst of treatment equipment is caused, the service life is shortened, and a pollutant gas escape event frequently occurs.
Disclosure of Invention
This section is intended to outline some aspects of embodiments of the utility model and to briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section as well as in the description summary and in the title of the application, to avoid obscuring the purpose of this section, the description summary and the title of the utility model, which should not be used to limit the scope of the utility model.
The present utility model has been made in view of the above and/or problems occurring in the prior art.
One of the purposes of the utility model is to provide a device for low-temperature denitration, desulfuration and VOC removal of flue gas, which can be integrated and has good effect on high-temperature and low-temperature industrial waste gas.
In order to solve the technical problems, the utility model provides the following technical scheme: a device for low-temperature denitration and desulfurization of flue gas and VOC removal, which comprises,
the adsorption bin is filled with porous adsorption media, and the flue gas directionally flows through the porous adsorption media in the direction of flowing through the porous adsorption media; the method comprises the steps of,
the desorption bin is intermittently communicated with the adsorption bin, and the porous adsorption medium can flow into the desorption bin from the adsorption bin;
the desorption bin has the characteristic of heating the porous adsorption medium, and is also provided with a desorption outlet.
As used herein, a "porous adsorption medium" refers to a material having a certain rigidity that can provide adsorption properties, and that can adsorb nitrogen oxides, sulfides, VOCs, and other compounds in flue gas. Common "rigid filter media" may be spherical or spheroid surface porous alumina, aluminum silicate, silica, carbide, and the like.
The term "directional flow-through" as used herein means that the flue gas moves in a fixed direction under a negative pressure and maintains the flow direction at all times. For example, from one side of the adsorption cartridge into and through the porous adsorption media before exiting from the other side of the adsorption cartridge.
The term "intermittent communication" as used herein means that the desorption cartridge and the adsorption cartridge are not always in a communication relationship (isolation relationship) but are communicated as required, and the communication relationship between the desorption cartridge and the adsorption cartridge is intermittent, i.e., is switched between the communication relationship and the isolation relationship throughout the process. For example, the desorption bin and the adsorption bin are communicated through a pipeline, a valve is arranged on the pipeline, and the communication relationship or the isolation relationship between the desorption bin and the adsorption bin is controlled through the valve.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the desorption bin is provided with a medium flow passage, and the porous adsorption medium directionally flows through the medium flow passage.
The term "media flow path" as used herein refers to a moving transport path of a porous adsorption media for providing a space for allowing sufficient desorption of adsorbed nitrogen oxides, sulfides, VOCs, and the like.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the desorption bin comprises a cylinder body and a rotating screw rod axially arranged along the cylinder body, and the medium flow passage is formed from the proximal end to the distal end of the screw rod.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the barrel is located below the adsorption bin, and the proximal end of the screw is located in the gravity direction of the porous adsorption medium.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the desorption outlet comprises a medium outlet and a gas outlet which are positioned at the far end of the screw, and the medium outlet is communicated with the top of the adsorption bin.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the porous adsorption medium is a rigid porous pellet with the diameter of 1-20 mm, the surface is a porous structure, the pore diameter of 1-20 mu m, the porosity of 50-90%, and the BET specific surface area of more than 400m 2 And/g, micropores and mesopores are mainly distributed on the surface of the sphere, so that the adsorption and desorption can be fast carried out. Because the pellets need to be transported and flowed, the pellets need to have corresponding impact strength which is more than 15 KJ/square meter. Because the pellets need to be reduced and desorbed in a high-temperature reduction screw machine, the pellets need to have corresponding high-temperature resistance and strength, the melting point of the material is more than 350 ℃, the heat deformation temperature is more than 350 ℃, the bending strength is more than 60MPa, and the tensile strength is more than 50MPa.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the rigid porous pellets are spherical or pellets or spheroids produced by metal salt calcination or polymer material synthesis, and have porous physical characteristics; and meanwhile, different pore opening agents are selected to generate the required pore diameter. The porous adsorption medium has the advantages of high strength, high temperature resistance, good wear resistance and no powder falling. The material can be selected from high molecular materials or materials such as alumina, zinc oxide, manganese oxide, silicon dioxide, aluminum silicate, diatomite, graphite, active coke, active carbon, carbon fiber, carbon nano tube, titanium dioxide, silicon carbide, silicon nitride and rare earth. Aluminum oxide, zinc oxide, manganese oxide are preferred.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: one side of the adsorption bin is communicated with an air inlet bin, the other side of the adsorption bin is communicated with an exhaust bin, and the adsorption bin is isolated from the air inlet bin and the exhaust bin through porous nets respectively;
the direction from the air inlet bin to the air outlet bin forms the directional flow-through direction of the flue gas.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the bottom of the air inlet bin is provided with an exhaust gas inlet, the top of the air inlet bin is closed, and the side part of the air inlet bin is communicated with the adsorption bin;
the top of the exhaust bin is provided with a clean gas outlet, the bottom of the exhaust bin is closed, and the side part of the exhaust bin is communicated with the adsorption bin.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the bottom width of the air inlet bin is smaller than the top width of the air inlet bin;
the width of the bottom of the exhaust bin is larger than the width of the top of the exhaust bin.
As a preferable scheme of the device for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the device comprises a plurality of waste gas treatment units consisting of an air inlet bin, an adsorption bin and an exhaust bin;
the flue gas is selectively communicated with an exhaust gas inlet of the air inlet bin;
the desorption bin is selectively communicated with the adsorption bin.
As referred to herein, "selectively communicating" refers to selectively communicating chambers as desired; the flue gas can selectively enter one or a plurality of air inlet cabins, the desorption cabins are selectively communicated with one or a plurality of adsorption cabins, wherein the waste gas treatment unit where the adsorption cabins communicated with the desorption cabins are positioned does not enter the flue gas, and the desorption reduction stage is realized.
Another object of the present utility model is to provide a method for low temperature denitration, desulfurization and VOC removal of flue gas, comprising,
the flue gas containing nitrogen oxides and sulfur dioxide enters an adsorption bin and flows through a porous adsorption medium to be discharged;
the porous adsorption medium after adsorption enters a desorption bin;
the desorption bin heats the porous adsorption medium, and the adsorbed nitrogen oxides and sulfur dioxide are removed from the porous adsorption medium and discharged from the desorption bin.
As a preferable scheme of the method for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the nitrogen oxides and the sulfur dioxide discharged from the desorption bin enter the removal bin, the nitrogen oxides and the sulfur dioxide can be subjected to desulfurization and denitrification treatment in the removal bin by spraying industrial conventional desulfurization and denitrification agents such as urea solution, hydrogen peroxide and the like, and the treated clean gas is emptied and dilute sulfuric acid is recovered; can also be used for desulfurizing and denitrating by respectively generating nitrate and sulfate through an acid-base neutralization method
As a preferable scheme of the method for low-temperature denitration, desulfurization and VOC removal of the flue gas, the utility model comprises the following steps: the porous adsorption medium is provided with a porous structure, and a catalyst is also attached in the porous structure of the porous adsorption medium;
the flue gas may also contain VOC gases;
the porous adsorption medium for adsorbing the VOC gas enters a desorption bin;
the desorption bin heats the porous adsorption medium, and the VOC gas is reduced into water and carbon dioxide by using a catalyst contained in the porous adsorption medium.
Compared with the prior art, the utility model has the following beneficial effects:
the device for low-temperature denitration, desulfurization and VOC removal of the flue gas provided by the utility model can be used for integrating denitration, desulfurization and VOC removal; the method has good effect on high-temperature and low-temperature industrial waste gas; the device is not affected by temperature, and can work at normal temperature and low temperature; can adapt to the instability of the exhaust gas amount in the industrial production, and does not need to consider the temperature change of the gas.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the drawings that are needed in the description of the embodiments will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present utility model, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art. Wherein:
FIG. 1 is a schematic structural diagram of embodiment 1 of the present utility model;
FIG. 2 is a schematic structural diagram of embodiment 2 of the present utility model;
FIG. 3 is a schematic structural diagram of embodiment 3 of the present utility model;
FIG. 4 is a schematic structural diagram of embodiment 4 of the present utility model;
FIG. 5 is a schematic structural diagram of embodiment 5 of the present utility model;
fig. 6 is a schematic flow chart in embodiment 5 of the present utility model.
Detailed Description
In order that the above-recited objects, features and advantages of the present utility model will become more apparent, a more particular description of the utility model will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present utility model, but the present utility model may be practiced in other ways other than those described herein, and persons skilled in the art will readily appreciate that the present utility model is not limited to the specific embodiments disclosed below.
Further, reference herein to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic can be included in at least one implementation of the utility model. The appearances of the phrase "in one embodiment" in various places in the specification are not necessarily all referring to the same embodiment, nor are separate or alternative embodiments mutually exclusive of other embodiments.
Example 1
As shown in fig. 1, in a first embodiment of the present utility model, the present embodiment provides a device for low-temperature denitration, desulfurization and VOC removal of flue gas, which mainly includes an adsorption bin 100 and a desorption bin 200, wherein the adsorption bin 100 is used for performing adsorption treatment on nitrogen oxides, sulfur dioxide and VOCs in flue gas through adsorption media, and the desorption bin 200 is used for performing desorption reduction treatment on adsorption saturated adsorption media.
Specifically, the adsorption bin 100 adopts a bin structure commonly used in the field of waste gas treatment, and the rest parts except for the part which needs to be connected with the outside are all closed structures. The adsorption bin 100 is filled with a porous adsorption medium S1, and the porous adsorption medium S1 selected in this embodiment is a rigid porous pellet, and the rigid porous pellet has a porous structure. The rigid porous pellets are calcined by metal salt or synthesized by polymer materials, and have porous physical characteristics; and meanwhile, different pore opening agents are selected to generate the required pore diameter. During the preparation, the catalyst required by the reduction reaction of VOC and nitrogen oxides can be added. The rigid porous pellets have the advantages of high strength, high temperature resistance, good wear resistance and no powder falling. Optionally alumina, zinc oxide, manganese oxide, silica, aluminum silicate, diatomaceous earth, graphite, activated coke, activated carbon, carbon fiber, carbon nanotube, titania, silicon carbide, silicon nitride, rare earth materials or mixtures of these materials. Preferably aluminum oxide, zinc oxide, manganese oxide or mixtures of these materials. The diameter of the rigid porous small ball is 1-20 mm; preferably 4 to 6mm.
The adsorption bin 100 further has a gas inlet 101 and a gas outlet 102, and the flue gas enters the adsorption bin 100 from the gas inlet 101 and flows through the porous adsorption medium S1, and is discharged from the gas outlet 102, and in this process, nitrogen oxides, sulfur dioxide, and VOCs in the flue gas are adsorbed by mesopores and micropores on the surface of the rigid porous pellets. The filling amount of the porous adsorption medium S1 in the adsorption bin 100 satisfies the requirement of sufficient contact with the entering flue gas, and generally, the rigid porous pellets are simply stacked in the adsorption bin 100 and fully filled.
The desorption bin 200 is a shell structure with an internal cavity, and the rest parts except the part which needs to be connected with the outside are all closed structures. The desorption bin 200 is communicated with the medium outlet 103 of the adsorption bin 100 through a pipeline, and the porous adsorption medium S1 can enter the desorption bin 200 from the medium outlet 103 of the adsorption bin 100 through the pipeline. The desorption bin 200 can heat the porous adsorption medium S1, a heating device can be arranged inside or outside the desorption bin 200, and the temperature of the internal space of the desorption bin 200 is raised through the heating device, so that the purpose of heating the filter medium S1 is achieved; naturally, conventional means such as microwaves, electromagnetism, heat conducting oil and the like can be adopted to heat or exchange heat to the porous adsorption medium S1, so that the purpose of heating the filter medium S1 is achieved.
After the porous adsorption medium S1 is heated, the adsorbed nitrogen oxides and sulfur dioxide are removed from micropores and mesopores of the pellets, and VOC gas is reduced into water and carbon dioxide in the micropores of the mesopores by utilizing the VOC-RCO catalyst contained in the pellets, and can be directly sprayed into the catalyst for VOC low-temperature oxidation in the cylinder. The removed high-concentration sulfur dioxide and nitrogen oxides are discharged from the gas outlet 204 of the desorption bin 200 to enter the subsequent nitrogen oxide and sulfur dioxide removal bin 205 for reaction, and the discharged gas has high concentration and high temperature, so that nitrate and sulfate can be generated simply by an acid-base neutralization method for recycling. The urea solution can also be sprayed, the conventional desulfurization and denitrification agent in the hydrogen peroxide industry can be sprayed, and the treated clean gas is emptied and the dilute sulfuric acid is recovered. And (5) evacuating the treated clean gas. The desorbed and reduced rigid porous pellets are discharged from the medium outlet 203 for collection and recycling. Or directly spraying reducing agents such as urea solution into the desorption bin 200, wherein hydrogen peroxide is used for respectively reducing the nitrogen oxides and the sulfur dioxide.
Example 2
As shown in fig. 2, this embodiment differs from the first embodiment in that the rigid porous pellets subjected to desorption reduction are recycled on-line.
The adsorption bin 100 is further provided with a medium inlet 104, and a medium outlet 203 of the desorption bin 200 is communicated with the medium inlet 104 through a pipeline, so that the desorbed and reduced rigid porous pellets are re-sent into the adsorption bin 100.
It should be noted that, the medium inlet 104 is disposed at the top of the adsorption bin 100, and the rigid porous pellets subjected to desorption and reduction enter the empty adsorption bin 100 from the medium inlet 104, so that the pellets can be naturally stacked under the action of gravity without additional energy.
Meanwhile, under the gravity action of the rigid porous pellets, the desorption bin 200 is arranged below the adsorption bin 100, particularly the medium discharge inlet 205 of the desorption bin 200 is arranged right below the medium outlet 103 of the adsorption bin 100, and the rigid porous pellets which are adsorbed with nitrogen oxides, sulfur dioxide and VOC can flow out of the adsorption bin 100 into the desorption bin 200 by means of gravity.
In order to realize continuous operation of recycling of the rigid porous pellets, a pellet storage tank 500 is arranged on a pipeline between the medium outlet 203 and the medium inlet 104, a certain amount of rigid porous pellets are pre-stored in the pellet storage tank 500, and the amount of the rigid porous pellets at least meets the amount of filling the adsorption bin 100 for one time; the media outlet 203 of the desorption cartridge 200 delivers the desorbed and reduced rigid porous pellets to the pellet storage tank 500 by conventional delivery means, such as positive pressure pumping, and the pellet storage tank 500 delivers the rigid porous pellets to the adsorption cartridge 100 by conventional delivery means, such as positive pressure pumping. When the pellet tank 500 is disposed above the adsorption bin 100, the transportation can be realized by the self weight of the rigid porous pellets, and the installation of a part of the transportation means can be reduced.
It should be noted that an electric control valve may be disposed on a pipeline (upper pipeline) between the pellet storage tank 500 and the adsorption bin 100, and a pipeline (lower pipeline) between the adsorption bin 100 and the desorption bin 200, to control the transfer of pellets and ensure the air tightness of the system. When the gas sensor equipped with the system detects that the concentration of the discharged gas is close to or exceeds a required index, an electric control valve of a lower pipeline is opened, and rigid porous pellets which are adsorbed with nitrogen oxides, sulfur dioxide and VOC flow out of the adsorption bin 100 by means of gravity; when the grating sensor of the electric control valve detects that no small ball flows out, the lower pipeline valve is closed, the upper pipeline electric control valve is opened, and the desorption and reduction rigid porous small ball flows into the adsorption bin 100 from the small ball storage tank 500 at the top by gravity. When the grating sensor of the electric control valve detects that the pellets are piled up in the adsorption bin 100, the electric control valve of the upper pipeline is closed, and the system continues to work; and the method is used as a process and is carried out reciprocally.
Example 3
As shown in fig. 3, this embodiment is different from the above embodiment in that the desorption cartridge 200 has a medium flow channel therein along which the porous adsorption medium S1 can flow in a directional manner. That is, the desorption chamber 200 has a certain distance between the medium discharge port 205 and the medium discharge port 203, and the porous adsorption medium S1 needs to be moved for a certain time from entering the desorption chamber 200 to being discharged, so that the adsorbed nitrogen oxides and sulfur dioxide are removed from micropores and mesopores of the pellets for a sufficient time, or the VOC gas reacts for a sufficient time by using the VOC-RCO catalyst contained in the pellets, and the purpose of sufficient desorption is achieved.
Based on this, the desorption cartridge 200 may specifically be constituted by a cylinder 201, the cylinder 201 having a certain axial length, the cylinder 201 may be a rectangular cylinder or a circular cylinder, preferably a circular cylinder; the cylinder 201 has a sealed airtight structure except for the portion to be connected to the outside. A heating block is laid outside the cylinder 201, and the inside of the cylinder 201 can be heated to 150-800 ℃; the temperature can be flexibly set according to the kind of the VOC-RCO catalyst contained in the pellets.
A screw 202 is disposed along the axial direction of the cylinder 201, the screw 202 is rotated by a motor and a speed reducer, and the proximal end to the distal end of the screw 202 form the medium flow path. The principle of operation of the screw 202 can be referred to in the prior art screw machines. Optionally single screw, twin screw, triple screw or quad screw, preferably single screw. Screw 202 primarily serves the functions of heat transfer and pellet transport.
The rigid porous pellets which adsorb nitrogen oxides, sulfur dioxide and VOC enter the near end of the screw 202, the inside of the cylinder 201 is heated to the desorption temperature, the screw 202 heats the rigid porous pellets to quickly transfer heat, so that the nitrogen oxides, sulfur dioxide are removed from micropores and mesopores of the pellets, and the VOC gas reacts into water and carbon dioxide in the mesopores and micropores when the temperature is increased to the working temperature of the catalyst by utilizing the VOC-RCO catalyst contained in the pellets. The catalyst for VOC low-temperature oxidation can also be directly sprayed into the cylinder. The removed high-concentration sulfur dioxide and nitrogen oxides are discharged from the gas outlet 204 of the desorption bin 200 to enter the subsequent nitrogen oxide and sulfur dioxide removal bin 205 for reaction, and the discharged gas has high concentration and high temperature, so that nitrate and sulfate can be generated simply by an acid-base neutralization method. And (5) evacuating the treated clean gas. The urea solution can also be sprayed, the conventional desulfurization and denitrification agent in the hydrogen peroxide industry can be sprayed, and the treated clean gas is emptied and the dilute sulfuric acid is recovered. The rigid pellets subjected to desorption and reduction are discharged from the medium discharge port 203 for collection and recycling. Reducing agents such as urea solution, hydrogen peroxide, can be directly sprayed into the cylinder 201 to reduce the nitrogen oxides and the sulfur dioxide. In order to enable rapid evacuation of the gas, a negative pressure device Q1 may be provided at the gas evacuation port 204.
Example 4
As shown in fig. 4, the difference between this embodiment and the above embodiment is that an air inlet bin 300 is provided on one side of the adsorption bin 100, an air outlet bin 400 is provided on the other side of the adsorption bin 100, the adsorption bin 100 is respectively communicated with the air inlet bin 300 and the air outlet bin 400, and the adsorption bin 100 is respectively isolated from the air inlet bin 300 and the air outlet bin 400 by a porous net S2. The flue gas enters the air inlet bin 300 from the exhaust gas inlet, flows through the adsorption bin 100 and is discharged from the clean gas outlet of the exhaust bin 400, namely, the direction from the air inlet bin 300 to the exhaust bin 400 forms the directional flow-through direction of the flue gas.
It should be noted that, to reduce the system resistance and save energy consumption, the exhaust gas inlet is disposed at the bottom 301 of the air inlet bin 300, the top 302 of the air inlet bin 300 is closed, and the side 303 of the air inlet bin 300 is in communication with the adsorption bin 100. The net gas outlet is arranged at the top 402 of the gas discharging bin 400, the bottom 401 of the gas discharging bin 400 is closed, and the side 403 of the gas discharging bin 400 is communicated with the adsorption bin 100.
Wherein the width of the bottom 301 of the air inlet bin 300 is smaller than the width of the top 302 thereof; in the inlet chamber 300, when the gas is introduced, the flow speed is reduced by changing the diameter from small to large, so that the influence of turbulence is reduced, and the gas flow uniformly passes through the adsorption chamber 100 in a laminar flow manner as much as possible.
A gas sensor can be further installed at the clean gas outlet of the exhaust bin 400 to detect the concentration of gas in real time; when the concentration exceeds the standard, the desorption reduction process in example 3 is performed. The width of the bottom 401 of the vent bin 400 is greater than the width of the top 402 thereof; in the air outlet bin 400, as the system is in a negative pressure state, a certain air flow resistance is formed in the air outlet bin 400 through the diameter change from large to small, so that the air flow speed in the air outlet bin is ensured to be stable, and the acquisition data of the air sensor is facilitated to be stable.
Example 5
As shown in fig. 5, the present embodiment is different from the above embodiment in that an air intake chamber 300, an adsorption chamber 100, and an exhaust chamber 400 are formed as one exhaust gas treatment unit; the present embodiment is formed by connecting a plurality of exhaust gas treatment units in parallel, each air inlet bin 300 is connected with one air inlet pipe M1 through an electric control valve, and each air outlet bin 400 is connected with one air outlet pipe M2 through an electric control valve. In addition, each adsorption bin 100 is connected to the desorption bin 200 through an electric control valve.
In addition, a dust particle filter can be installed at the front end of the air inlet pipe M1 to filter and remove dust and particles.
It should be noted that, according to the amount of the incoming gas, the electric control valve controls the operation of the adsorption bins 100 to adapt to the non-uniformity of the incoming gas in the production environment, so as to maximally reduce the energy consumption.
In order to further improve the utilization rate of the bin, as shown in fig. 5, the air inlet bins 300 and the air outlet bins 400 may be alternately arranged, the adsorption bins 100 are disposed between the adjacent air inlet bins 300 and air outlet bins 400, and the waste gas entering the air inlet bins 300 can pass through the adsorption bins 100 from the left side and the right side respectively and then enter the air outlet bins 400, and then the clean gas is collected by the air outlet bins 400 and finally discharged.
Specifically, as shown in fig. 6, the workflow of the present embodiment is as follows:
after the waste gas containing nitrogen oxides, sulfur dioxide and VOC passes through a dust particle filter at the front end to remove dust and particles, or the industrial waste gas generated by the front-stage production equipment does not contain dust particles; the number of the bin operation can be adjusted according to the air intake amount and the pollutant concentration, for example, the number of the bin needing to be operated can be automatically calculated according to the air intake amount and the pollutant concentration through a PLC (programmable logic controller), and the bin operation is automatically adjusted; the service time of the filter medium is prolonged, and the energy consumption is saved. When the gas is conveyed to the bottom of each air inlet bin 300 by the air inlet pipe M1, the gas passes through the metal porous net from the left side and the right side and then enters the adsorption bin 100, and nitrogen oxides, sulfur dioxide and VOC are adsorbed by mesopores and micropores on the surfaces of the rigid porous pellets; the gas after passing through the adsorption bin 100 does not contain or meets the emission standard and enters the exhaust bin 400.
The top of the exhaust bin 400 is connected with an exhaust pipe M2, and the treated clean air or the air meeting the emission standard is exhausted into the atmosphere through a negative pressure exhaust fan Q2.
The gas sensor at the gas purifying outlet at the top of the gas exhausting bin 400 detects that the concentration of the exhausted gas is close to or exceeds a required index, an electric control valve of a pipeline between the adsorption bin 100 and the desorption bin 200 is opened, and rigid porous pellets of adsorbed nitrogen oxides, sulfur dioxide and VOC flow out of the adsorption bin 100 by means of gravity; when the grating sensor of the electric control valve detects that no small ball flows out, the pipeline valve between the adsorption bin 100 and the desorption bin 200 is closed, the electric control valve of the pipeline between the small ball storage tank 500 and the adsorption bin 100 is opened, and the rigid porous small ball subjected to desorption and reduction flows into the adsorption bin 100 from the small ball storage tank 500 at the top by means of gravity. When the grating sensor of the electric control valve detects that the pellets are piled up in the adsorption bin 100, the electric control valve of the pipeline between the pellet storage tank 500 and the adsorption bin 100 is closed, and the system continues to work; and the method is used as a process and is carried out reciprocally. Because the system is connected with a plurality of bins in parallel, the time for replacing the small balls is controlled to be about 3-5 minutes.
The rigid porous pellets which adsorb nitrogen oxides, sulfur dioxide and VOC enter the near end of the screw 202, the inside of the cylinder 201 is heated to the desorption temperature, the screw 202 heats the rigid porous pellets to quickly transfer heat, so that the nitrogen oxides, sulfur dioxide are removed from micropores and mesopores of the pellets, and VOC gas is reduced into water and carbon dioxide in the mesopores and micropores by utilizing the VOC-RCO catalyst contained in the pellets. The removed high-concentration sulfur dioxide and nitrogen oxides are discharged from the gas outlet 204 of the desorption bin 200 to enter a subsequent nitrogen oxide and sulfur dioxide removal bin for reaction, and the discharged gas has high concentration and high temperature, so that nitrate and sulfate can be generated simply by an acid-base neutralization method. And (5) evacuating the treated clean gas. The desorbed and reduced rigid porous pellets are sent to a pellet storage tank 500.
Example 6
As shown in fig. 5, an exhaust gas treatment test was performed on the apparatus for low-temperature denitration, desulfurization and VOC removal of flue gas provided in example 5. For the convenience of statistics, the chambers of the device are numbered, the adsorption chambers are eliminated, only the air inlet chambers and the air outlet chambers are numbered, the first air outlet chamber close to the air inlet direction is numbered 1#, the first air inlet chamber close to the air inlet direction is numbered 2#, and so on until the final numbers of 2n-1# and 2n are obtained.
The rigid porous pellets filled in the adsorption bin are made of aluminum oxide and aluminum silicate, the diameter of the rigid porous pellets is between 4 and 6mm, the surface of the rigid porous pellets is of a porous structure, micropores and mesopores are mainly distributed on the surface of a sphere, the pore diameter is between 1 and 20 mu m, the porosity is 70%, and the BET specific surface area is more than 400m 2 /g; the physical properties of the rigid porous pellets were: impact strength > 15KJ/m 2 Melting point of material is higher than 500 deg.C, heat distortion temperature>Bending strength at 350 DEG C>60MPa, tensile Strength>50MPa. The rigid porous pellets were good in appearance and free of surface damage.
After removing particulate dust from flue gas containing nitrogen oxides, sulfur dioxide and VOC, the concentrations of the nitrogen oxides, the sulfur dioxide and the VOC are respectively 200mg/m 3 、100mg/m 3 、50mg/m 3 The gas temperature is 100 ℃, the gas is sent into an air inlet bin of the equipment, and the average speed of the waste gas passing through an adsorption bin is controlled to be 0.05m/s.
According to formula s=v/0.05; wherein V is the gas supply amount per unit time; s is the required filtration adsorption area. And calculating a bin needing to be worked, and calculating 2 air inlet bins and 3 air outlet bins by a system. That is, in example 6, only the chambers 1 to 5# in fig. 5 were opened, and the other chambers were closed for intake and exhaust.
The nitrogen oxides, sulfur dioxide, and VOC concentrations in the # 1, # 3, and # 5 chambers after 24 hours of treatment are shown in table 1.
TABLE 1
The equipment is operated for 24 hours, and the average concentration value of the chambers # 2 and # 4 rises by 30 percent; starting to run a process of replacing the rigid porous pellets, and allowing the pellets adsorbed with the gas to enter a desorption bin; the clean rigid porous pellets are replenished to the adsorption bin for continued operation.
Heating the cylinder body of the desorption bin to 300 ℃, and running the screw at a low speed of 50 revolutions per minute; after 3 minutes, take offThe detection value of the VOC sensor in the attached bin is 1500mg/m from the highest peak value 3 Reduced to 0-5 mg/m 3 Indicating that VOC is catalyzed and decomposed in the cylinder.
The gas outlet of the desorption bin is opened to discharge the removed high-concentration sulfur dioxide and nitrogen oxides, and the high-concentration sulfur dioxide and nitrogen oxides enter the removal bin to carry out catalytic reaction of the nitrogen oxides and sulfur dioxide; and when the nitrogen oxides and the sulfur dioxide are not detected in the removal bin, the gas in the bin is exhausted.
And conveying the rigid porous pellets treated in the desorption bin to a pellet storage tank for standby. Clean rigid porous pellets in a pellet storage tank are periodically sampled, detected by solvent extraction and GC-MS (mass spectrometry), and an extract obtained after 3 hours of extraction at 60 ℃ by using a dichloromethane solvent is subjected to GC-MS analysis, so that no nitrogen oxide, sulfur dioxide and VOC residues are found on the surface.
Example 7
Referring to example 6, an exhaust gas treatment test was performed on the apparatus for low temperature denitration, desulfurization and VOC removal of flue gas provided in example 5. The equipment and the rigid porous pellets are the same, and after the flue gas containing nitrogen oxides, sulfur dioxide and VOC is subjected to particulate matter dust removal, the concentrations of the nitrogen oxides, the sulfur dioxide and the VOC are respectively 100 mug/m 3 、20ug/m 3 、120ug/m 3 The gas temperature is 30 ℃, the gas is sent into an air inlet bin of the equipment, and the average speed of the waste gas passing through an adsorption bin is controlled to be 0.1m/s.
According to formula s=v/0.1; wherein V is the gas supply amount per unit time; s is the required filtration adsorption area. And calculating the chambers needing to be worked, and carrying out systematic calculation, wherein 1 air inlet chamber and 2 air outlet chambers need to be worked. That is, in example 7, only the chambers 1 to 3# in fig. 5 were opened, and the other chambers were closed for intake and exhaust.
The nitrogen oxides, sulfur dioxide, VOC concentrations in the # 1 and # 3 chambers are shown in table 2, after 96 hours of treatment.
TABLE 2
The equipment is operated for 96 hours, and the average concentration value of the No. 2 bin is increased by 20 percent; starting to run a process of replacing the rigid porous pellets, and allowing the pellets adsorbed with the gas to enter a desorption bin; the clean pellets are replenished to the adsorption bin for continuous operation.
Heating the cylinder body of the desorption bin to 250 ℃, and running the screw at a low speed of 50 revolutions per minute; after 3 minutes, the detection value of the VOC sensor in the desorption bin is 1000mg/m from the highest peak value 3 Reduced to 0-5 mg/m 3 Indicating that VOC is catalyzed and decomposed in the cylinder.
The gas outlet of the desorption bin is opened to discharge the removed high-concentration sulfur dioxide and nitrogen oxides, and the high-concentration sulfur dioxide and nitrogen oxides enter the removal bin to carry out catalytic reaction of the nitrogen oxides and sulfur dioxide; and when the nitrogen oxides and the sulfur dioxide are not detected at the outlet of the removal bin, the gas in the bin is exhausted.
And conveying the rigid porous pellets treated in the desorption bin to a pellet storage tank for standby. Clean rigid porous pellets in a pellet storage tank are periodically sampled, detected by solvent extraction and GC-MS (mass spectrometry), and an extract obtained after 3 hours of extraction at 60 ℃ by using a dichloromethane solvent is subjected to GC-MS analysis, so that no nitrogen oxide, sulfur dioxide and VOC residues are found on the surface.
The device for low-temperature denitration, desulfurization and VOC removal of the flue gas provided by the utility model can be used for integrating denitration, desulfurization and VOC removal; has good effect on high-temperature and low-temperature industrial waste gas.
Compared with the existing SCR denitration and desulfurization equipment and RCO-VOC removal equipment, the minimum working temperature of the existing SCR denitration and desulfurization equipment is 150 ℃; the minimum operating temperature of the RCO-VOC removal device is 200 degrees celsius. The utility model is not affected by temperature, and can work at normal temperature and low temperature.
The utility model can adapt to the instability of the exhaust gas amount in industrial production, and does not need to consider the temperature change of the gas. Can work in different temperature areas; solves the problem that SCR denitration and desulfurization equipment and RCO-VOC removal equipment cannot work at low temperature. Solves the problems of unstable gas quantity change and catalyst poisoning failure of SCR denitration and desulfurization equipment and RCO-VOC removal equipment.
When the porous adsorption medium in the adsorption bin reaches a set value or a saturation value, the utility model can dynamically replace the filter medium without stopping production or reducing production load and affecting emission index. The pollutant is adsorbed on the porous adsorption medium, and when the porous adsorption medium is used for desorbing the pollutant gas in the reduction screw machine, the heat transfer efficiency is higher than that of the metal surface-gas due to the heat transfer of the metal-metal oxide-porous medium-gas; can be quickly desorbed, and saves energy.
As micropores and mesopores used for adsorption are controlled to be on the surface of an object in the production process, the filter medium with pore channels on the surface and the inside is easier to be desorbed rapidly. Time and energy consumption are saved.
The reduction reaction is carried out in the screw machine, so that the reduction temperature can be quickly set according to working conditions, the efficiency is high, and the operation energy consumption is low.
It should be noted that the above embodiments are only for illustrating the technical solution of the present utility model and not for limiting the same, and although the present utility model has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present utility model may be modified or substituted without departing from the spirit and scope of the technical solution of the present utility model, which is intended to be covered in the scope of the claims of the present utility model.
Claims (10)
1. The utility model provides a flue gas low temperature denitration desulfurization and get rid of VOC's device which characterized in that: comprising the steps of (a) a step of,
the adsorption bin (100), porous adsorption media (S1) are filled in the adsorption bin (100), and flue gas directionally flows through in the direction of flowing through the porous adsorption media (S1);
the desorption bin (200), desorption bin (200) with adsorption bin (100) intermittent type nature intercommunication, porous adsorption medium (S1) can follow adsorption bin (100) inflow desorption bin (200), desorption bin (200) have to porous adsorption medium (S1) heating' S characteristic, desorption bin (200) still are equipped with the desorption discharge port.
2. The device for low-temperature denitration, desulfurization and VOC removal of flue gas according to claim 1, wherein: the desorption bin (200) is provided with a medium flow passage, and the porous adsorption medium (S1) directionally flows along the medium flow passage.
3. The device for low-temperature denitration, desulfurization and VOC removal of flue gas according to claim 2, wherein: the desorption bin (200) comprises a barrel (201) and a rotary screw rod (202) axially arranged along the barrel (201), and the medium flow channel is formed from the proximal end to the distal end of the screw rod (202).
4. The device for low-temperature denitration, desulfurization and VOC removal of flue gas according to claim 3, wherein: the barrel (201) is located below the adsorption bin (100), and the proximal end of the screw (202) is located in the gravity direction of the porous adsorption medium (S1).
5. The apparatus for low temperature denitration, desulfurization and VOC removal of flue gas according to claim 3 or 4, wherein: the desorption outlet comprises a medium outlet (203) and a gas outlet (204) which are positioned at the far end of the screw (202), and the medium outlet (203) is communicated with the top of the adsorption bin (100).
6. The device for low-temperature denitration, desulfurization and VOC removal of flue gas according to claim 5, wherein: the porous adsorption medium (S1) is a rigid porous pellet, and the rigid porous pellet has a porous structure.
7. The apparatus for low temperature denitration, desulfurization and VOC removal of flue gas according to any one of claims 1 to 4 and 6, characterized in that: one side of the adsorption bin (100) is communicated with an air inlet bin (300), the other side of the adsorption bin (100) is communicated with an exhaust bin (400), and the adsorption bin (100) is isolated from the air inlet bin (300) and the exhaust bin (400) through porous nets (S2) respectively;
the direction from the air inlet bin (300) to the air outlet bin (400) forms the directional flow-through direction of the flue gas.
8. The device for low-temperature denitration, desulfurization and VOC removal of flue gas according to claim 7, wherein: the bottom (301) of the air inlet bin (300) is provided with an exhaust gas inlet, the top (302) of the exhaust gas inlet is closed, and the side part (303) of the air inlet bin (300) is communicated with the adsorption bin (100);
the top (402) of the exhaust bin (400) is provided with a clean gas outlet, the bottom (401) of the clean gas outlet is closed, and the side (403) of the exhaust bin (400) is communicated with the adsorption bin (100).
9. The device for low-temperature denitration, desulfurization and VOC removal of flue gas according to claim 8, wherein: the width of the bottom (301) of the air inlet bin (300) is smaller than the width of the top (302) of the air inlet bin;
the width of the bottom (401) of the exhaust bin (400) is larger than the width of the top (402) of the exhaust bin.
10. The apparatus for low temperature denitration, desulfurization and VOC removal of flue gas according to claim 8 or 9, characterized in that: comprises a plurality of waste gas treatment units consisting of the air inlet bin (300), the adsorption bin (100) and the exhaust bin (400);
the flue gas is selectively communicated with an exhaust gas inlet of the air inlet bin (300);
the desorption bin (200) is selectively communicated with the adsorption bin (100).
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| CN202320412772.0U CN219463017U (en) | 2023-03-07 | 2023-03-07 | Device for low-temperature denitration and desulfurization of flue gas and VOC removal |
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