CN111249881A - Glass kiln flue gas treatment method and system - Google Patents
Glass kiln flue gas treatment method and system Download PDFInfo
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- CN111249881A CN111249881A CN202010115202.6A CN202010115202A CN111249881A CN 111249881 A CN111249881 A CN 111249881A CN 202010115202 A CN202010115202 A CN 202010115202A CN 111249881 A CN111249881 A CN 111249881A
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- 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
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- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
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- 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
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- 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
- B01D53/90—Injecting reactants
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0241—Other waste gases from glass manufacture plants
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Abstract
The invention provides a glass kiln flue gas treatment method, which comprises the following steps: primary waste heat recovery, wherein the waste heat of the glass kiln flue gas is recovered by a primary heat exchanger; performing dry modulation, namely adding excessive alkaline powder into the glass kiln flue gas subjected to the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas; catalyzing by using a ceramic membrane, wherein the glass kiln flue gas modulated by the dry method passes through a ceramic membrane catalysis filter tube under an alkaline condition, and performing catalytic treatment to obtain treated dischargeable glass kiln flue gas; wherein, the ceramic membrane catalysis filter tube includes: the catalyst layer comprises an active component, a carrier cocatalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer. The invention also provides a glass kiln flue gas treatment system.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a glass kiln flue gas treatment method and a glass kiln flue gas treatment system.
Background
In the glass production process, flue gas components are very complicated due to the addition of mirabilite and soda ash, and the denitration, desulfurization and dust removal are affected. The glass kiln is fired once every 15 to 20 minutes, and the contents of sulfur dioxide, smoke dust and nitrogen oxides are all changed violently in the process of firing; in the glass production process, the stability of kiln pressure is very important, and the whole set of desulfurization, denitration and dust removal equipment is arranged at the tail part of the smoke of the melting furnace. Along with the continuous improvement of the flue gas emission standard of the glass melting furnace and the continuous emergence of the monitoring measures of the strict atmospheric pollutant emission in various regions in China, the ultralow emission standard is imperative. Especially glass furnaces, have high nitrogen oxides, high sulfur dioxide, and contain multi-component impurities that are difficult to meet emission standards.
In the related art, the tail gas of the glass melting furnace is usually treated by adopting a mode of electrostatic dust collection + Selective Catalytic Reduction (SCR) denitration + wet desulphurization + wet dust collection, or an electrostatic dust collection + SCR denitration + dry desulphurization + bag dust collection.
However, the electrostatic precipitator has a complex structure, unstable dust removal efficiency, high investment cost for desulfurization, and incomplete dust removal, and is difficult to meet the requirements of increasingly severe emission standards.
Disclosure of Invention
The invention provides a glass kiln flue gas treatment method and a glass kiln flue gas treatment system, which aim to solve the problems that an electrostatic dust collector in the related art is complex in structure, unstable in dust removal efficiency, high in desulphurization investment cost, incomplete in dust removal and difficult to meet the requirements of increasingly severe emission standards.
In order to achieve the above object, according to a first aspect of the present invention, there is provided a glass kiln flue gas treatment method, comprising:
primary waste heat recovery, wherein the waste heat of the glass kiln flue gas is recovered by a primary heat exchanger;
performing dry modulation, namely adding excessive alkaline powder into the glass kiln flue gas subjected to the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas;
catalyzing by using a ceramic membrane, wherein the glass kiln flue gas modulated by the dry method passes through a ceramic membrane catalysis filter tube under an alkaline condition, and performing catalytic treatment to obtain treated dischargeable glass kiln flue gas; wherein, the ceramic membrane catalysis filter tube includes: the catalyst layer comprises an active component, a carrier cocatalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer.
In an alternative embodiment, the catalyst comprises TiO in a component ratio of 780:90:5:30:75:15:10:12、WO3、MoO3、V2O5、SiO2、Al2O3CaO and Na2O, or TiO2、WO3、MoO3、V2O5、SiO2、Al2O3CaO and K2O; wherein, the V2O5As the active component, the TiO2、WO3、MoO3As a co-catalyst component of the carrier, SiO2、Al2O3CaO and Na2O, or SiO2、Al2O3CaO and K2O is the mechanically stabilizing component.
In an optional embodiment, the dry tempering, which adds an excess amount of alkaline powder to the glass kiln flue gas after the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas, comprises:
and adding excessive calcium hydroxide powder into the glass kiln flue gas subjected to the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas.
In an optional embodiment, the molar ratio of the calcium hydroxide powder to the sulfur dioxide content is 1:1.2 to 1: 1.8.
In an optional embodiment, the ceramic membrane catalysis, in which the glass kiln flue gas after being modulated by the dry method passes through a ceramic membrane catalysis filter tube under an alkaline condition, and the ceramic membrane catalysis is performed to obtain a treated dischargeable glass kiln flue gas, includes:
and spraying a proper amount of ammonia water into the glass kiln flue gas modulated by the dry method according to the content of the nitric oxide in the glass kiln flue gas, and mixing the ammonia water with the glass kiln flue gas.
In an alternative embodiment, after the ceramic membrane catalyzed, alkaline condition, the glass kiln flue gas after the dry conditioning is passed through a ceramic membrane catalytic filter tube for catalytic treatment to obtain a treated dischargeable glass kiln flue gas, the method further comprises:
and secondary waste heat recovery, wherein the treated glass kiln flue gas which can be discharged is subjected to waste heat recovery through a secondary heat exchanger.
In an optional embodiment, after the ceramic membrane-catalyzed and the glass kiln flue gas subjected to the dry-process modulation passes through a ceramic membrane-catalyzed filter tube under an alkaline condition and is subjected to catalytic treatment to obtain a treated dischargeable glass kiln flue gas, the method further comprises:
and (4) performing ash circulation treatment, wherein the filtered substances obtained by filtering and intercepting the waste liquor by the ceramic membrane catalytic filter tube are circulated to the dry method for modulation.
According to a second aspect of the present invention, there is provided a glass kiln flue gas treatment system, comprising:
the primary heat exchanger is used for recovering the waste heat of the glass kiln flue gas;
the static mixer is used for mixing the glass kiln smoke and the alkaline powder;
the ceramic membrane filtering catalyst is used for filtering the glass kiln flue gas and carrying out catalytic treatment on the glass kiln flue gas under an alkaline condition to obtain dischargeable stripping kiln flue gas; the ceramic membrane catalytic filter tube comprises: the catalyst layer comprises an active component, a carrier cocatalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer.
In an alternative embodiment, the system further comprises:
and the secondary heat exchanger is used for recovering the waste heat of the glass kiln flue gas after the ceramic membrane filtration and catalysis treatment.
In an alternative embodiment, the system further comprises:
an inlet of the ash bin is communicated with the static mixer and the ceramic membrane filtering catalyst and is used for collecting residual ash of the static mixer and the ceramic membrane filtering catalyst;
and the outlet of the ash storehouse is communicated with the inlet of the static mixer and is used for conveying ash to the static mixer, and alkaline powder is added into the static mixer.
The invention provides a glass kiln flue gas treatment method and a glass kiln flue gas treatment system, wherein the glass kiln flue gas treatment method comprises the following steps: primary waste heat recovery, wherein the waste heat of the glass kiln flue gas is recovered by a primary heat exchanger; dry-process modulation, namely adding excessive alkaline powder into the glass kiln flue gas subjected to primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas; catalyzing by using a ceramic membrane, namely, under the alkaline condition, allowing the glass kiln flue gas modulated by the dry method to pass through a ceramic membrane catalysis filter tube for catalytic treatment to obtain treated glass kiln flue gas which can be discharged; wherein, ceramic membrane catalysis chimney includes: the catalyst layer comprises an active component, a carrier cocatalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer. Therefore, through primary waste heat recovery, the flue gas temperature is reduced while the flue gas heat recovery is improved, and the desulfurization is conveniently carried out by dry-process modulation at the later stage; during dry blending, excessive alkaline powder is added and reacts with acid gas in the flue gas, so that the desulfurization efficiency is improved; under the alkaline condition, the flue gas is denitrated under the action of the catalyst by effectively utilizing the waste heat of the flue gas through the catalysis of the ceramic membrane, and the alkaline powder filtered and intercepted by the ceramic membrane can be reused for dry modulation, so that the dry modulation cost is reduced, the denitration efficiency is improved, and the glass kiln flue gas treatment cost is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a flow chart of an implementation of a glass kiln flue gas treatment method provided in an embodiment of the present application;
fig. 2 is a schematic structural diagram of a dry modulation system provided in an embodiment of the present application;
FIG. 2a is an enlarged schematic structural diagram of an atomizing device in a dry-process modulating system according to an embodiment of the present application;
FIG. 2b is a top view of an atomizing device in the dry brewing system according to the embodiment of the present application;
FIG. 2c is a front view of a blade in a dry modulation system according to an embodiment of the present application;
FIG. 2d is a left side view of a blade in a dry modulation system according to an embodiment of the present application;
FIG. 3 is a schematic structural view of a ceramic membrane filtration catalyst according to an embodiment of the present disclosure;
FIG. 3a is a schematic diagram of a pulse back-blowing device in a ceramic membrane filtration catalyst in accordance with an embodiment of the present invention;
FIG. 3b is an enlarged view of a portion of FIG. 3 a;
FIG. 4 is a flow chart of an implementation of a glass kiln flue gas treatment method according to another embodiment of the present application;
fig. 5 is a schematic structural diagram of a glass kiln flue gas treatment system provided in the embodiment of the present application.
The reference numbers in the figures illustrate:
1-a flue gas treatment system;
10-a primary heat exchanger;
20-dry modulation system;
21-basic powder feeder;
22-an ammonia addition device;
221-an atomizing device;
23-a static mixer;
231-blades;
30-ceramic membrane filtration catalyst;
31-a pulse back-blowing device;
32-ceramic membrane catalytic tubes;
321-a ceramic filter layer;
322-a catalytic layer;
40-a secondary heat exchanger;
50-ash storehouse.
With the above figures, certain embodiments of the invention have been illustrated and described in more detail below. The drawings and written description are not intended to limit the scope of the inventive concepts in any manner, but rather to illustrate the concepts of the disclosure to those skilled in the art by reference to specific embodiments.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature.
In the description of the present invention, it should be noted that unless otherwise specifically stated or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning a fixed connection, an indirect connection through intervening media, a connection between two elements, or an interaction between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the description of the present invention, it is to be understood that the terms "top", "bottom", "side wall", "upper", "lower", "left", "right", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, are only for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
In the description of the present invention, "a plurality" means two or more unless specifically stated otherwise.
Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
Fig. 1 is a flow chart of an implementation of a glass kiln flue gas treatment method provided in an embodiment of the present application. Fig. 2 is a schematic structural diagram of a dry modulation system provided in an embodiment of the present application. Fig. 2a is an enlarged schematic structural diagram of an atomizing device in a dry-process modulation system according to an embodiment of the present application. Fig. 2b is a top view of an atomizing device in the dry brewing system according to the embodiment of the present application. Fig. 2c is a front view of a blade in the dry modulation system according to the embodiment of the present application. Fig. 2d is a left side view of a blade in the dry modulation system according to the embodiment of the present application. Fig. 3 is a schematic structural diagram of a ceramic membrane filtration catalyst according to an embodiment of the present application. Fig. 3a is a pulse back-blowing device in a ceramic membrane filtration catalyst according to an embodiment of the present application. Fig. 3b is a partially enlarged schematic view of a portion a in fig. 3 a.
Referring to fig. 1, an embodiment of the present application provides a glass kiln flue gas treatment method, including the following steps:
In specific implementation, the glass kiln flue gas treatment method provided by the embodiment of the application is used for treating high-temperature flue gas generated by a natural gas oxy-fuel combustion glass kiln; specifically, the temperature of the flue gas generated by the glass kiln for natural gas oxy-fuel combustion is 800-900 ℃, and the flue gas enters the primary waste heat recovery. Specifically, in this application embodiment, the primary waste heat recovery system may be a heat exchanger, specifically may be a plate heat exchanger, a shell and tube heat exchanger, or a heat exchanger in other forms, and the specific form of the heat exchanger in this application embodiment is not limited. The glass kiln gas entering the heat exchanger exchanges heat with the heat exchange medium in the heat exchanger. In some optional embodiments, the heat exchange medium may be water, and after heat exchange, the heat exchange medium is heated for domestic heating and other purposes. Through one-level waste heat recovery, the heat carried in the flue gas of the glass kiln is effectively recovered, the energy utilization efficiency is improved, and the production cost is effectively reduced.
And step 102, performing dry modulation, namely adding excessive alkaline powder into the glass kiln flue gas subjected to primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas.
Specifically, in the embodiment of the application, the temperature of the flue gas of the glass kiln subjected to primary waste heat recovery is reduced to 350-380 ℃, and the flue gas of the glass kiln enters a dry-method modulation system.
Specifically, in the dry conditioning system 20, as shown in fig. 2, an excessive amount of alkaline powder is added to the flue gas of the glass kiln through an alkaline powder feeder 21, the excessive amount of alkaline powder reacts with the acidic gas such as sulfur dioxide, hydrogen chloride, hydrogen fluoride and the like in the flue gas, and the fumes such as sulfur dioxide, hydrogen chloride, hydrogen fluoride, heavy metals and the like in the flue gas finally form solid particles, thereby removing the acidic gas in the flue gas.
Specifically, in the embodiment of the present application, in the dry-process preparation system 20, while adding an excessive amount of alkaline powder to the flue gas, an appropriate amount of ammonia water is sprayed into the flue gas through the materialization apparatus by the ammonia adding device 22. Specifically, in the embodiment of the present application, the amount of the ammonia water is determined according to the concentration of the nitrogen oxide in the flue gas, and in an optional embodiment, the molar ratio of the ammonia water to the nitrogen oxide is 1: 0.9. When sprayed into the flue by the atomizer 221, the ultra-fine ammonia droplets are rapidly mixed 23 with the flue gas by the static mixer.
Specifically, the atomizing device 221 includes an atomizing mixing chamber and double-arc-shaped spray holes, the liquid and the compressed air enter the atomizing mixing chamber through the spray pipe, and the spray pipe is connected with the high-efficiency atomizing device through threads and is sprayed out from the double-arc-shaped spray holes. The atomizing device 221 has the advantages of simple structure, uneasy blockage, easy maintenance and capability of adjusting the particle size of the fog drops by changing the pressure of the compressed air.
More specifically, referring to fig. 2a to 2d, in the embodiment of the present application, the static mixer 23 includes a plurality of blades 231, and when the flue gas flows upwards in the static mixer 23, the flue gas pushes the blades 231, so that the blades 231 rotate, and the flue gas and the ultra-fine ammonia mist are rapidly mixed; in the embodiment of this application, through static mixer 23, utilize the mobile propulsion mixture aqueous ammonia of flue gas and flue gas, need not additionally provide the energy, when having improved the efficiency that flue gas and aqueous ammonia mix, reduced the consumption of energy, reduced the treatment cost to the flue gas.
The invention provides a glass kiln flue gas treatment method, which improves the recycling of flue gas heat and reduces the flue gas temperature through primary waste heat recovery, and is convenient for later-stage dry-process modulation for desulfurization; during dry blending, excessive alkaline powder is added and reacts with acid gas in the flue gas, so that the desulfurization efficiency is improved; under the alkaline condition, the flue gas is denitrated under the action of the catalyst by effectively utilizing the waste heat of the flue gas through the catalysis of the ceramic membrane, and the alkaline powder filtered and intercepted by the ceramic membrane can be reused for dry modulation, so that the dry modulation cost is reduced, the denitration efficiency is improved, and the glass kiln flue gas treatment cost is reduced.
Fig. 4 is a flow chart of an implementation of a glass kiln flue gas treatment method according to another embodiment of the present application.
Based on the foregoing embodiment, referring to fig. 4, another embodiment of the present application provides a glass kiln flue gas treatment method, including the following steps:
step 401, primary waste heat recovery, wherein the glass kiln gas is subjected to waste heat recovery through a primary heat exchanger.
And step 402, performing dry blending, namely adding excessive alkaline powder into the glass kiln flue gas subjected to primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas.
Specifically, according to the content of sulfur dioxide in the flue gas of the glass kiln, excessive calcium hydroxide powder is added into the flue gas of the glass kiln after primary waste heat recovery.
In some alternative embodiments, the molar ratio of calcium hydroxide powder to sulfur dioxide content is 1:1.2 to 1: 1.8. Optionally, in a specific embodiment, the molar ratio of calcium hydroxide powder to sulfur dioxide content is 1: 1.5.
specifically, in this embodiment, after the calcium hydroxide powder is added to the dry blending system, the calcium hydroxide powder reacts with the acidic gas in the flue gas as follows:
SO2+Ca(OH)2=CaSO3+H2O；
2CaSO3+O2=2CaSO4；
SO3+Ca(OH)2=CaSO4+H2O；
2HCl+Ca(OH)2=CaCl2+2H2O；
2HF+Ca(OH)2=CaF2+2H2O；
the sulfur dioxide, hydrogen fluoride, hydrogen chloride, heavy metal and other smoke in the flue gas finally react to form solid particles.
Specifically, in the embodiment of the present application, in the dry-process preparation system 20, while adding an excessive amount of alkaline powder to the flue gas, an appropriate amount of ammonia water is sprayed into the flue gas through the materialization apparatus by the ammonia adding device 22. Specifically, in the embodiment of the present application, the amount of the ammonia water is determined according to the concentration of the nitrogen oxide in the flue gas, and in an optional embodiment, the molar ratio of the ammonia water to the nitrogen oxide is 1: 0.9. When sprayed into the flue by the atomizer 221, the ultra-fine ammonia droplets are rapidly mixed 23 with the flue gas by the static mixer. After the ammonia water and the flue gas are completely mixed, the mixture of the ammonia water and the flue gas enters the ceramic membrane filtration catalyst 30.
Specifically, in the examples of the application, the catalyst comprises TiO with the mass component ratio of 780:90:5:30:75:15:10:12、WO3、MoO3、V2O5、SiO2、Al2O3CaO and Na2O, or TiO2、WO3、MoO3、V2O5、SiO2、Al2O3CaO and K2O; wherein, V2O5As an active component, TiO2、WO3、MoO3As a carrier co-catalyst component, SiO2、Al2O3CaO and Na2O, or SiO2、Al2O3CaO and K2O is a mechanically stable component.
After the flue gas components are filtered by the ceramic filter layer 321 of the ceramic membrane catalytic tube 32, the smoke dust and the excessive calcium hydroxide powder in the flue gas are filtered and concentrated in the ash hopper at the bottom of the ceramic membrane filtration catalytic device 30 for recycling. The flue gas enters the ceramic membrane catalysis tube 32 after being filtered to contact with the catalysis layer 322, and under the action of the catalyst and the flue gas self-contained waste heat, the flue gas and ammonia water are subjected to the following reduction reaction:
4NO+4NH3+O2=4N2+6H2O；
2NO2+4NH3+O2=3N2+6H2O；
so that the nitrogen oxides in the flue gas and the ammonia water are subjected to reduction reaction under the action of the catalyst to be removed.
In some optional embodiments, the ceramic membrane filtration catalyst 30 further includes a pulse back-flushing device 31, specifically, after the ceramic membrane filtration catalyst 30 works for a period of time, the pulse back-flushing device 31 performs back-flushing on the ceramic membrane catalyst tube 32, so as to avoid the risk that the ceramic membrane catalyst tube 32 is blocked, and ensure effective work of the ceramic membrane catalyst tube 32.
And step 404, secondary waste heat recovery, wherein the treated dischargeable glass kiln flue gas is subjected to waste heat recovery through a secondary heat exchanger.
Specifically, the secondary waste heat recovery system may be a heat exchanger, specifically, a plate heat exchanger, a shell and tube heat exchanger, or another heat exchanger, and the specific form of the heat exchanger is not limited in the embodiment of the present application. The glass kiln gas entering the heat exchanger exchanges heat with the heat exchange medium in the heat exchanger. In some optional embodiments, the heat exchange medium may be water, and after heat exchange, the heat exchange medium is heated for domestic heating and other purposes. Through second grade waste heat recovery, effectively retrieved the heat that carries in the glass kiln flue gas in this application embodiment, improved energy utilization efficiency, effectively reduced manufacturing cost.
And 405, performing ash circulation treatment, and circulating a filtrate obtained by filtration and interception of the ceramic membrane catalytic filter tube to a dry method for modulation.
Specifically, the ash filtered by the ceramic filter layer 321 contains excessive calcium hydroxide powder, and the ash enters the dry-method modulation system again for recycling, so that the use of the calcium hydroxide powder is effectively saved, and the treatment cost is saved.
Compared with the traditional process, the processing method adopted by the embodiment of the application has the following process advantages:
1) pollutant removal efficiency is high, when the flue gas passes through ceramic membrane catalysis filter tube, carry out high-efficient desorption to smoke and dust, HF, HCl, dioxin and heavy metal, alkali metal component, the smoke and dust is not more than 5mg/Nm year, and the flue gas carries out the denitration through soaking the ceramic membrane filter inner wall of SCR catalyst after the purification, and the denitration is efficient, and ammonia escape is low, realizes that the nitride is long-term stable ultralow to be discharged.
2) The ceramic membrane catalytic filter tube has long service life and easy operation and maintenance, and can ensure that the service life of the SCR catalyst is longer than that of the traditional process because the ceramic membrane catalytic filter tube carries out early-stage high-efficiency pre-removal on acidic substances, alkali metals and dust which are easy to cause catalyst poisoning.
3) The system collects the flue gas desulfurization, denitration, defluorination and dust removal into an integrated high-efficiency purification device, and has the advantages of simple process flow, small occupied area and easy operation and maintenance.
4) The system adopts a specially designed static mixer to realize the high-efficiency uniform mixing of gas-solid and gas-gas, thereby not only greatly improving the reaction efficiency, but also effectively controlling the escape of ammonia and saving the cost of chemical reagents and fuel for users.
The system has simple process flow, small temperature drop of the whole system, small pressure loss, maximized utilization of waste heat by users and low operating cost.
Specifically, by comparison with the conventional process, refer to tables 1 and 2 below; wherein, the table 1 is a traditional process flue gas purification condition table; table 2 shows the flue gas purification conditions of the glass kiln flue gas treatment method provided in the embodiment of the present application.
TABLE 1 flue gas cleaning situation chart of traditional process
As can be seen from table 1, the flue gas of the glass kiln is treated by the traditional method of "two-electric-field high-temperature electrostatic dust removal + SCR denitration + limestone/lime-gypsum desulfurization technique + wet electric dust removal", and the ultra-low emission standard cannot be met.
Table 2 table of flue gas purification conditions of glass kiln flue gas treatment method provided in the embodiment of the present application
As can be seen from the table 2, the glass wine bottle melting furnace smoke treatment process using natural gas as fuel adopts technical improvement aiming at the exceeding standard of smoke (dust), the original oxygen-enriched combustion process is reserved, the new process is the processes of oxygen-enriched combustion, primary waste heat, dry tempering, ceramic membrane catalytic filtration and secondary waste heat, and the ultra-low emission standard is achieved.
Fig. 5 is a schematic structural diagram of a glass kiln flue gas treatment system provided in the embodiment of the present application.
Based on the foregoing embodiment, referring to fig. 5, an embodiment of the present application provides a glass kiln flue gas treatment system 1, including:
the primary heat exchanger 10 is used for recovering the waste heat of the flue gas of the glass kiln;
a static mixer 23 for mixing the glass kiln gas with the alkaline powder;
the ceramic membrane filtering catalyst 30 is used for filtering the glass kiln flue gas and performing catalytic treatment on the glass kiln flue gas under an alkaline condition to obtain dischargeable stripping kiln flue gas; the ceramic membrane catalytic filter tube 32 comprises: the catalyst layer 322 comprises an active component, a carrier auxiliary catalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer.
In an optional implementation manner, the flue gas treatment system 1 provided in the embodiment of the present application further includes:
and the secondary heat exchanger 40 is used for recovering the waste heat of the glass kiln flue gas after the ceramic membrane filtration and catalysis treatment.
In an optional implementation manner, the flue gas treatment system 1 provided in the embodiment of the present application further includes:
the ash bin 50 is communicated with the static mixer 23 and the ceramic membrane filtering catalyst 30 through an inlet of the ash bin 50 and is used for collecting residual ash of the static mixer and the ceramic membrane filtering catalyst;
the outlet of the ash silo 50 communicates with the inlet of the static mixer 23 for conveying ash to the static mixer 23, adding alkaline powder to the static mixer 23.
The system provided by the embodiment of the application has the following advantages:
1) simultaneously has the functions of desulfurization, denitrification and dust removal;
2) the smoke removal rate can reach 99.9995%, and the removal rate of smoke and aerosol with the particle size of 0.1 mu m, which cannot be removed by the traditional process, is over 99%, so that the escape of ammonia in the form of aerosol can be greatly reduced;
3) high temperature resistance, corrosion resistance, washing resistance, high mechanical strength, stable structure, no deformation and long service life;
4) the heat is preserved in a totally-enclosed way, the temperature is reduced by 20-30 ℃, the heat preservation and insulation are excellent, and the utilization rate of waste heat is high;
5) the consumption of cooling water and air is low;
6) the modular design has high integration level and small occupied area, and is easy to transport and install;
7) intelligent control, flexibility and simple and convenient use and operation;
8) high efficiency, energy saving, low operation cost and wide application range.
It should be noted that the present embodiment has the same or corresponding beneficial effects as the previous embodiment, and the description of the present embodiment is omitted.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. The glass kiln flue gas treatment method is characterized by comprising the following steps:
primary waste heat recovery, wherein the waste heat of the glass kiln flue gas is recovered by a primary heat exchanger;
performing dry modulation, namely adding excessive alkaline powder into the glass kiln flue gas subjected to the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas;
catalyzing by using a ceramic membrane, wherein the glass kiln flue gas modulated by the dry method passes through a ceramic membrane catalysis filter tube under an alkaline condition, and performing catalytic treatment to obtain treated dischargeable glass kiln flue gas; wherein, the ceramic membrane catalysis filter tube includes: the catalyst layer comprises an active component, a carrier cocatalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer.
2. The method of claim 1, wherein the catalyst comprises TiO in a ratio of 780:90:5:30:75:15:10:1 components2、WO3、MoO3、V2O5、SiO2、Al2O3CaO and Na2O, or TiO2、WO3、MoO3、V2O5、SiO2、Al2O3CaO and K2O; wherein, the V2O5As the active component, the TiO2、WO3、MoO3As a co-catalyst component of the carrier, SiO2、Al2O3CaO and Na2O, or SiO2、Al2O3CaO and K2O is the mechanically stabilizing component.
3. The method according to claim 1, wherein the dry tempering by adding an excess amount of alkaline powder to the glass kiln flue gas after the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas comprises:
and adding excessive calcium hydroxide powder into the glass kiln flue gas subjected to the primary waste heat recovery according to the content of sulfur dioxide in the glass kiln flue gas.
4. The method according to claim 3, wherein the molar ratio of the calcium hydroxide powder to the sulfur dioxide content is 1:1.2 to 1: 1.8.
5. The method according to claim 1, wherein the ceramic membrane catalysis is performed to catalytically treat the glass kiln flue gas modulated by the dry method through a ceramic membrane catalysis filter tube under an alkaline condition to obtain a treated dischargeable glass kiln flue gas, and the method comprises the following steps:
and spraying a proper amount of ammonia water into the glass kiln flue gas modulated by the dry method according to the content of the nitric oxide in the glass kiln flue gas, and mixing the ammonia water with the glass kiln flue gas.
6. The method according to claim 1, wherein after the ceramic membrane catalyzed, dry conditioned glass kiln flue gas is catalytically treated by passing through a ceramic membrane catalyzed filter tube under alkaline conditions to obtain treated dischargeable glass kiln flue gas, the method further comprises:
and secondary waste heat recovery, wherein the treated glass kiln flue gas which can be discharged is subjected to waste heat recovery through a secondary heat exchanger.
7. The method according to claim 1, wherein the ceramic membrane catalysis is performed, and after the glass kiln flue gas after the dry conditioning is subjected to catalytic treatment by a ceramic membrane catalysis filter tube under an alkaline condition to obtain a treated dischargeable glass kiln flue gas, the method further comprises:
and (4) performing ash circulation treatment, wherein the filtered substances obtained by filtering and intercepting the waste liquor by the ceramic membrane catalytic filter tube are circulated to the dry method for modulation.
8. A glass kiln flue gas treatment system, comprising:
the primary heat exchanger is used for recovering the waste heat of the glass kiln flue gas;
the static mixer is used for mixing the glass kiln smoke and the alkaline powder;
the ceramic membrane filtering catalyst is used for filtering the glass kiln flue gas and carrying out catalytic treatment on the glass kiln flue gas under an alkaline condition to obtain dischargeable stripping kiln flue gas; the ceramic membrane catalytic filter tube comprises: the catalyst layer comprises an active component, a carrier cocatalyst component and a mechanical stabilizing component, and the catalyst is uniformly distributed in the ceramic filter layer.
9. The system of claim 8, further comprising:
and the secondary heat exchanger is used for recovering the waste heat of the glass kiln flue gas after the ceramic membrane filtration and catalysis treatment.
10. The system of claim 8, further comprising:
an inlet of the ash bin is communicated with the static mixer and the ceramic membrane filtering catalyst and is used for collecting residual ash of the static mixer and the ceramic membrane filtering catalyst;
and the outlet of the ash storehouse is communicated with the inlet of the static mixer and is used for conveying ash to the static mixer, and alkaline powder is added into the static mixer.
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