KR101946355B1 - Flame-free air purification apparatus using oxidation catalyst and explosion-proof atmosphere purification system including the same - Google Patents

Abstract

Disclosed are a flame-free air purification apparatus using an oxidation catalyst and an explosion-proof air purification system including the same. The air purification apparatus includes: a frame; a gas inflow module fixed in the frame, and including a first inflow port for taking fuel gas and air and a second inflow port for taking fuel gas and harmful gas; a primary mixing member installed in the upper part of the gas inflow module, and mixing gases rising from the gas inflow module; an oxidation catalyst module stacked on the gas inflow module to be connected to the module, and filled with an oxidation catalyst for decomposing the harmful gas with radiant heat by an oxidation catalyst action; an internal preheater installed in the oxidation catalyst module to make contact with the oxidation catalyst, and activating the oxidation catalyst action by providing a heat source to the oxidation catalyst; a connecting chamber module stacked on the oxidation catalyst module to be connected to the module to take high-temperature oxidation gas from the oxidation catalyst module; and an exhaust stack connected to the inside of the connecting chamber module to discharge the oxidation gas in the connecting chamber module to the outside.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a flame-based air purification apparatus and an explosion-proof atmosphere purification system using the same,

More particularly, the present invention relates to an apparatus for purifying an air, and more particularly, to an apparatus for removing by-product gas and noxious gas by employing a high-temperature oxidation catalyst, The present invention relates to a flame-based air purification apparatus using a high-temperature oxidation catalyst characterized by the fact that the air-fuel ratio is switched to a safety mode for preventing explosion at the time of operation and an explosion-proof atmosphere purification system including the same.

Exhaust gases from various factories include various hazardous chemicals such as volatile organic compounds (VOCs), which are the main cause of air pollution, and gases causing odor. The above-mentioned volatile organic compounds may be various kinds, but aromatic compounds such as benzene and phenol, hydrocarbon compounds such as alkane and alkene, halogen such as chlorine, ) Compounds, heterogeneous hydrocarbons including nitrogen, oxygen, and the like. Major sources of volatile organic compounds include paints, paints and plastics, chemical plants, refineries, petroleum refineries and dry cleaners.

These volatile organic compounds cause tropospheric ozone pollution, stratospheric destruction, and global warming depending on their type and reaction form in the atmosphere. When exposed to volatile organic compounds in humans, plants and animals, they cause respiratory diseases and neurological disorders in the short term , In the long term it can cause cancer, gene mutation, and the like. As such, emissions of volatile organic compounds, which are very harmful to health itself, are increasing every year due to the development of industry, and environmental pollution is further increased accordingly.

On the other hand, odor is mainly caused by air pollution and stimulates the smell of the person. Aldehydes, indoles, ketones, alcohols, phenols, chlorine compounds, carbon disulfide, ammonia, organic acids and the like are also present in addition to hydrogen sulfide, mercaptans and amines. In such places as rubber manufacturing factory, drug manufacturing factory, plastic manufacturing factory, food manufacturing factory, fertilizer factory, paper making factory, etc., which are made from such odor materials as raw materials, enrichment industry, sewage disposal plant, crematorium, garbage landfill A large amount of odor is generated.

When a person stinks, mental stress builds up first, and psychological discomfort leads to irritability, hysteria, and insomnia. Physiologically, symptoms such as an increase in blood pressure due to smell, abnormalities of the reproductive system caused by changes in hormone secretion, smell decline, headache, and vomiting may also occur.

In order to remove such harmful chemical substances and odor substances, it is conventionally necessary to use a regenerative thermal oxidation (RTO) apparatus of a direct combustion method, a regenerative catalytic oxidation (RCO) apparatus of an indirect combustion method, Biofilters and the like were mainly used

The RTO device is a method in which the exhaust gas is directly burned and oxidized, and then the heat of combustion is recovered and reused. Since the RTO device is economical to treat a volatile organic compound having a high treatment efficiency and a high concentration, it is widely used today. However, if the equipment cost is too high and the concentration of volatile organic compounds is low, it is not economical because the operation cost is high. Also, it is not suitable for the treatment of volatile organic compounds containing halogen or sulfur compounds, Follow.

The RCO apparatus is advantageous in that the catalyst is burned to activate, then reacted with the exhaust gas to treat the exhaust gas, and the combustion heat is recovered and reused, the operation cost is low, the generation of nitrogen compounds (NOx) is small and the apparatus is compact. However, the facility cost is higher than that of the RTO device, its application range is limited according to the generation of the gas to be treated, it is not suitable for treatment of volatile organic compounds having a high flow rate fluctuation or high concentration, and the catalyst should be periodically replaced.

On the other hand, the adsorption treatment apparatus treats the exhaust gas by contacting the adsorbent with a solid adsorbent, collecting and collecting the volatile organic compounds on the surface of the adsorbent, and regenerating the adsorbent by desorption using a heat cycle. This is advantageous in that the removal efficiency of volatile organic compounds is high and the fuel cost is low. However, a pretreatment facility for filtering the particulate matter contained in the exhaust gas is required, and waste water is generated during the regeneration of the adsorbent, There are disadvantages.

In the case of a biofilter, it is difficult to use it in the case of a substance which is not biodegradable. When the biofilter is installed, it takes a long time to react biologically, so it occupies a lot of site, is difficult to maintain and maintain activity on microorganisms, and is particularly sensitive to temperature, resulting in low efficiency in winter and difficult operation.

Further, although a method of removing contaminants using a plasma treatment process has been widely used, there is a problem that extremely small particulate contaminants are not removed even by plasma treatment because they are very small in size. In order to solve such a problem, recently, a technique has been developed in which water is atomized into a small particulate pollutant to spray particulates to coagulate the particulate matter, followed by electrostatic dust collection. However, since water has a polar nature, it is difficult to remove pollutants having a non-polar nature because the pollutants having polar nature can be coarsened.

In addition, if the coarsening is caused by water to a certain level or higher, by-products that cause free fall occur, and there is a problem that extra cost is incurred in processing the by-products.

Therefore, it is required to develop an efficient and economical method for removing harmful substances which are harmful to human body, odor and environmental pollution, but which are not treated in general pollutant removal process.

Patent Document 1: Registration No. 10-0817303 Patent Document 2: JP-A-10-0737941 Patent Document 3: Registration Patent No. 10-0929905

SUMMARY OF THE INVENTION It is an object of the present invention to provide a flame-based air purification apparatus using an oxidation catalyst having a high efficiency of removing by-product gas and harmful gas as a high-temperature oxidation catalyst is employed.

It is another object of the present invention to provide a flame-proof (heater-heated) air purification apparatus that uses an oxidation catalyst capable of reducing the amount of oxidation catalyst by adopting the flame-proof system and capable of downsizing the apparatus.

It is another object of the present invention to provide an explosion-proof type air purification system which is switched to a safety mode for preventing explosion during abnormal operation of the apparatus through constant interception of temperature and pressure in the apparatus.

It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory and are not intended to limit the invention to the precise form disclosed. There will be.

In order to achieve the above-mentioned object, A gas inlet module fixed to the frame and having a first inlet port through which fuel gas and air are introduced and a second inlet port through which fuel gas and noxious gas are introduced; A primary mixing member provided at an inner upper portion of the gas inlet module to mix gases raised from the gas inlet module; An oxidation catalyst module which is stacked to communicate with the gas inflow module and is filled with an oxidation catalyst for decomposing noxious gas by radiant heat due to oxidation catalysis; An internal preheating heater installed inside the oxidation catalyst module so as to be in contact with the oxidation catalyst to provide a heat source to the oxidation catalyst to activate oxidation catalyst operation; A connecting chamber module which is stacked so as to communicate with the oxidation catalyst module and into which high temperature oxidizing gas flows from the oxidation catalyst module; And an exhaust stack provided to communicate with the inside of the connecting chamber module and for discharging the oxidizing gas in the connecting chamber module to the outside, wherein a flameless atmosphere purification apparatus using a high temperature oxidation catalyst is provided.

Preferably, the apparatus further comprises a secondary mixing member interposed between the gas inlet module and the oxidation catalyst module to mix the primary mixed gas again by the primary mixing member, wherein the secondary mixing member is a mesh, . ≪ / RTI >

The apparatus may further include an external preheater which surrounds the outside of the oxidation catalyst module and provides a heat source to the oxidation catalyst to activate the oxidation catalyst function.

The exhaust heat recovery module may further include a waste heat recovery module installed in the connection stack connecting the connecting chamber module and the exhaust stack and collecting the waste heat from the hot oxidizing gas passing through the connection stack.

Preferably, the connection stack is formed by connecting a first connection stack on the side of the oxidation catalyst module and a second connection stack on the exhaust stack side, the waste heat recovery module being in communication with the first and second connection stacks, A plurality of heat exchange pipes; A heat exchanging pipe, a flange joined between the first and second connection stacks, a refrigerant for cooling the heat exchange pipe is filled therein, a refrigerant inlet for introducing the refrigerant and a refrigerant outlet for discharging the refrigerant, Lt; / RTI >

Preferably, the internal preheating heater may be any one of an electric heater and an explosion-proof heater.

Preferably, each module can be joined by flange jointing.

Preferably, the adsorption module may further include an adsorption module disposed between the connecting chamber module and the exhaust stack, the adsorption module being filled with an adsorbent material for adsorbing harmful substances contained in the oxidizing gas.

Preferably, the oxidation catalyst can be a hexaaluminate-based catalyst having a transition metal.

Preferably, the transition metal component may comprise at least one of manganese, cobalt, iron or chromium.

Preferably, the oxidation catalyst comprises a nitrate transition metal, an alkaline earth metal and an aluminum nitrate, wherein the alkaline earth metal may comprise at least one of calcium, strontium, barium or radium.

Preferably, the molar ratio of the nitrate transition metal / alkaline earth metal / aluminum nitrate is (1-x) / (1-y) / 11, where x is a number in the range of 0.1 to 0.5 and y is a number in the range of 0.1 to 0.5 .

Preferably, the amount of CO (carbon monoxide) discharged from the oxidation catalyst module may be 20 ppm or less.

Preferably, the NO _x released from the oxidation catalyst module The amount can be 20 ppm or less.

Preferably, the treatment efficiency of the noxious gas and the by-product gas can be 99% or more.

Preferably, the noxious gas and the by-product gas may include a volatile organic compound species including a petroleum gas, a sulfur compound type, an ammonia compound, and a halogen compound.

In another embodiment of the present invention, there is provided a flame-based air purification apparatus using the above-described high-temperature oxidation catalyst, wherein when the internal temperature of the oxidation catalyst module is higher than a set temperature, cooling air is supplied into the gas- A primary cooling means for allowing the supplied cooling air to be discharged to the oxidation catalyst module or the exhaust stack; Secondary cooling means for supplying cooling air to the connecting chamber module and discharging the supplied cooling air to the exhaust stack when the internal temperature of the oxidation catalyst module is higher than the set temperature by the cooling action by the primary cooling means; The present invention also provides an explosion-proof atmosphere purifying system.

Preferably, the primary cooling means comprises: a first cooling fan operated when the internal temperature of the oxidation catalyst module is higher than the set temperature; A first cooling air supply line connecting between the first cooling fan and the gas inflow module to supply the cooling air of the first cooling fan to the inside of the gas inflow module; A first supply valve for selectively opening and closing the first cooling air supply line; A first cooling air exhaust line connecting between the gas inlet module and the exhaust stack to exhaust the cooling air supplied to the interior of the gas inlet module to the exhaust stack; And a first exhaust valve selectively opening the first cooling air exhaust line.

Preferably, the secondary cooling means includes a second cooling fan operated when the internal temperature of the oxidation catalyst module is higher than the set temperature even by the operation of the primary cooling means; A second cooling air supply line connecting between the second cooling fan and the connecting chamber module for supplying the cooling air of the second cooling fan to the inside of the connecting chamber module; A second supply valve for selectively opening and closing the second cooling air supply line; And a second cooling air exhaust line connecting between the connecting chamber module and the exhaust stack for discharging the cooling air supplied into the connecting chamber module to the exhaust stack.

Preferably, first pressure regulating means for regulating the supply pressure of the noxious gas supplied to the interior of the atmospheric purification apparatus to a constant level; And second pressure regulating means for regulating the pressure inside the atmospheric air purifying apparatus to a constant level.

Preferably, the first pressure regulating means includes a first pressure regulating valve installed on the noxious gas supply line for regulating the air pressure of the noxious gas supplied to the gas inflow module of the atmospheric purifier uniformly; And a second bypass line for bypassing an overpressure higher than a set pressure of the supplied noxious gas to the exhaust stack, and the second pressure regulating means comprises a connection for connecting the gas inflow module of the atmospheric purification device and the exhaust stack line; And a second pressure regulating valve installed on the connecting line for discharging an overpressure exceeding the set pressure to the exhaust stack when the internal pressure of the gas inflowing module is higher than the set pressure.

Preferably, a harmful gas bypass line for bypassing the noxious gas introduced into the noxious gas supply line to the exhaust stack; And a bypass line open / close valve for selectively opening and closing the noxious gas bypass line.

According to the embodiment of the present invention, the efficiency of removing by-product gas and noxious gas is excellent by employing a high-temperature oxidation catalyst.

In addition, since each component is modularized, necessary units can be selectively laminated and exchanged easily.

In addition, since the non-flammable system using an electric heater is adopted, the consumption amount of the oxidation catalyst for fuel can be reduced, and the maintenance cost can be reduced, which is advantageous for miniaturization.

In addition, safety factors such as temperature and pressure of the device are detected in real time, and safety mode is switched to safety mode to normalize temperature and pressure during abnormal operation.

It should be understood that the effects of the present invention are not limited to the above effects and include all effects that can be deduced from the detailed description of the present invention or the configuration of the invention described in the claims.

1 is a perspective view of a flame-based air purification apparatus using an oxidation catalyst according to an embodiment of the present invention;
2 is a cross-sectional view of a flame-based air purification apparatus using an oxidation catalyst according to an embodiment of the present invention
3 is a cross-sectional view of a flame-based air purification apparatus using an oxidation catalyst according to another embodiment of the present invention
FIG. 4 is a block diagram of an air purifying system according to the present invention.
FIG. 5 is a block diagram of an air purifying system according to the present invention.
Fig. 6 is a configuration diagram of an air purifying system according to the present invention.

The invention may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. In order to clearly illustrate the present invention in the drawings, portions not related to the description are omitted, and like reference numerals are given to similar portions throughout the specification.

Throughout the specification, when a part is referred to as being "connected" (connected, connected, coupled) with another part, it is not only the case where it is "directly connected" "Is included. Also, when an element is referred to as "comprising ", it means that it can include other elements, not excluding other elements unless specifically stated otherwise.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The singular expressions include plural expressions unless the context clearly dictates otherwise. In this specification, the terms "comprises" or "having" and the like refer to the presence of stated features, integers, steps, operations, elements, components, or combinations thereof, But do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, or combinations thereof.

Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings.

First, the air purifying apparatus will be described.

FIG. 1 is a perspective view of a flameless-type air purifying apparatus using an oxidation catalyst according to an embodiment of the present invention, FIG. 2 is a cross-sectional view of a flameless-type air purifying apparatus using an oxidation catalyst according to an embodiment of the present invention And FIG. 3 is a cross-sectional view of a flame-based air purification apparatus using an oxidation catalyst according to another embodiment of the present invention.

1 to 3, a flame-based air purification apparatus (hereinafter referred to as an "air purification apparatus") 100 using an oxidation catalyst according to an embodiment of the present invention includes a frame 110, a gas An inlet module 120, a primary mixing member 130, an oxidation catalyst module 140, an internal preheater 150, a connecting chamber module 160 and an exhaust stack 170. Here, each module can be laminated by flange jointing, which facilitates additional lamination and reduction of modules.

The frame 110 has a rectangular lattice shape and supports the air purifier 100. In this embodiment, a base having a height adjuster and a caster may be provided on the bottom of the frame 110 have.

The gas inflow module 120 is fixed to the frame 110 and serves to introduce fuel gas, noxious gas, and air. The first inflow port 121 is provided at one side thereof with a fuel gas and air introduced thereinto And a second inflow port 122 through which fuel gas and noxious gas are introduced may be provided on the other side.

Here, the harmful gas (by-product gas) may include volatile organic compounds including petroleum gas, sulfur compounds, ammonia compounds, and halogen compounds.

The primary mixing member 130 serves to primarily mix fuel gas and noxious gas rising from the gas inflow module while being provided inside the gas inflow module 120. In this embodiment, The mixing member 130 may be formed in the form of a drawstock semi-woven with iron filaments. In this case, the fuel gas and the harmful gas are mixed well while passing through the irregular channel of the iron-semi-

The oxidation catalyst module 140 is for catalytic oxidation. The oxidation catalyst module 140 is stacked on the gas inflow module 120 so as to communicate with the oxidation catalyst 141. The oxidation catalyst 141 is filled with an oxidation catalyst 141 for decomposing harmful gas by radiant heat . Although not shown, an observation window may be provided on one side of the oxidation catalyst module 140 so that the oxidation state of the oxidation catalyst 141 can be visually confirmed and observed.

Processing efficiency of the self-test results, CO (carbon monoxide), the amount discharged from the catalytic oxidation module 140 is 20ppm or less, the NO _X amount of 20ppm or less discharged from the catalytic oxidation module 140, a by-product gas and a harmful gas is 99% Respectively.

The oxidation catalyst 141 may be in a granular form, that is, in a pellet form, but a cylindrical form, a cylindrical form, a spherical form, or a hexagonal form may be applied. When the pores are formed, the fuel gas is prevented from diffusing and being prevented from being pressurized, so that the fuel gas passes through the fuel gas without passing through the specific region.

Preferably, the size of the pellet is 2 to 5 mm. If the size of the pellet is larger than this range, the pore between the pellet and the pellet becomes large and the oxidation efficiency lowers. Similarly, if the size of the pellet is smaller than this range, the pore becomes small and the passing rate of the fuel gas lowers, Therefore, the size range should be adhered to.

On the other hand, the high-temperature oxidation catalyst 141 can be mass-produced through the following processes.

Namely, as a first step, a metal precursor solution containing a nitrate transition metal, an alkali earth metal and aluminum nitrate is prepared. The molar ratio of nitrate transition metal / alkaline earth metal / aluminum nitrate is (1-x) / (1-y) / 11 wherein x is a number in the range of 0.1 to 0.5 and y can range in the range of 0.1 to 0.5 . The nitrate transition metal may comprise at least one of manganese, cobalt, iron or chromium. The alkaline earth metal may comprise at least one of calcium, strontium, barium or radium. The preparation of the metal precursor solution may be by dissolving nitrate transition metal, alkaline earth metal and aluminum nitrate in distilled water.

In two steps, a precipitation solution is prepared. The preparation of the precipitation solution may be by stirring the element in distilled water. The concentration of urea in the precipitation solution may be 12 times the concentration of the metal precursor in the metal precursor solution.

In step 3, the metal precursor solution and the precipitating solution are mixed, and when the mixed solution is prepared, the mixed solution is heated to 90 to 100 ° C.

Keep in 4 steps for 10 ~ 48 hours so that precipitation reaction occurs. The precipitation reaction of the mixed solution can be performed by a uniform solution precipitation method.

In step 5, the precipitate slurry formed by the precipitation reaction is filtered and separated from the mixed solution. The separated mixed solution by filtration of the precipitate slurry can be recycled to produce a precipitate solution.

In step 6, the precipitate slurry is washed.

In step 7, drying is performed to remove moisture in the washed precipitate slurry. The washed precipitate slurry may be dried at a temperature in the range of 100 to 150 ° C.

Firing is carried out at 1,000 to 1,500 ° C to remove moisture remaining in the dried slurry of precipitate. The calcined precipitate slurry has a hexaaluminate structure and can have a specific surface area ranging from 5 to 150 m ² / g.

The uniform solution precipitation method applied to the method for producing a high-temperature oxidation catalyst according to the present invention is simple in process, unlike other precipitation methods, and is easy to design a process for mass production. The co-precipitation method widely used as a general catalyst preparation method uses a basic substance such as sodium carbonate (Na ₂ CO ₃ ) or sodium hydroxide (NaOH) as a precipitant for synthesizing a catalyst, and the metal precursor uses an acidic substance such as metal nitrate do. The salt produced in the acid neutralization reaction of these two materials is used as a catalyst. In this process, pH control is one of the important factors determining the properties and performance of the catalyst. However, adjusting the rate of pH control is a relatively difficult process and a tricky process. It is relatively difficult to produce catalysts of the same quality in large quantities and repeatedly due to such processes.

The uniform solution precipitation method used in the method for producing a high-temperature oxidation catalyst according to the present invention can produce a high-temperature oxidation catalyst of the same quality in a large amount and repeatedly while solving such pH control problem. In the uniform solution precipitation method, the element used as a precipitant is decomposed into ammonia (NH ₃ ) and carbon dioxide gas (CO ₂ ) at a temperature of 90 to 100 ° C. and reacts with metal precursors. At this time, the precipitation reaction appears uniformly throughout the solution, and the pH naturally remains at 7. In the coprecipitation method using sodium hydroxide or the like as a precipitant, the precipitation reaction locally takes place first in the place where the precipitant is introduced, It is difficult to produce a catalyst of the same quality because it is difficult to ensure homogeneity. On the other hand, the uniform solution precipitation method can solve such a problem, so that a high-temperature oxidation catalyst of the same quality can be relatively easily produced.

In the co-precipitation method using sodium hydroxide or the like as a precipitant in the filtration and washing process, impurities such as sodium (Na) or nitrate remaining in the slurry of the precipitate are removed, and these impurities are removed only by dissolving in a large amount of distilled water. These impurities act as a cause of deterioration of the physical properties and performance of the catalyst, and therefore filtration and washing processes must be strictly carried out. The amount of distilled water used is 3 to 4 times higher than that of distilled water used for synthesizing the catalyst. On the other hand, the impurities produced in the uniform solution precipitation method are ammonium nitrate (NH ₄ NO ₃ ) or unreacted elements, Are easily dissolved in a small amount of distilled water and can be removed by heat. Therefore, the homogeneous solution precipitation method hardly exhibits the physical properties and performance degradation of the catalyst due to the impurities as compared with the common coprecipitation method, and the process cost can be reduced due to the simplicity of the process.

In addition, after the precipitation reaction, most of the wastewater produced in the filtration process is unreacted, and thus can be reused as a precipitating solution serving as a precipitant. In the precipitation reaction, only the same precursor concentration as the precursor concentration is used for the precipitation reaction, and the remaining elements remain. The reason why the excess element is used is to proceed the precipitation reaction rate toward the reaction well. Only a portion of the solution is used, and the remainder is returned to the filtrate as it is. If only the theoretically used amount of element is added to the filtrate, it can be recycled as a precipitate solution.

And the washing process is easier than the conventional coprecipitation method. The reason for this is that impurities remaining in the precipitate after the filtration process remain in the form of ammonium nitrate produced after the reaction. Ammonium nitrate is also highly soluble and can be sufficiently removed even by using only about 1/2 of the distilled water used for the reaction. It can be completely removed in the process. In addition, the small amount of wastewater generated here is also reusable. Thus, the method of manufacturing a high-temperature oxidation catalyst according to an embodiment of the present invention can be said to be a pollution-free manufacturing method with almost no waste liquid to be discarded.

In the drying and firing process, the drying of the slurry of the precipitate proceeds at about 100 DEG C for at least 10 hours to remove residual moisture. In the firing process, the firing is maintained at 1,000 ° C. or more for about 1 hour or more, so that a high-temperature oxidation catalyst capable of maintaining performance and durability even at a high temperature can be manufactured.

Hereinafter, a method for producing a high-temperature oxidation catalyst according to the present invention will be described in detail.

1. Preparation of metal precursor solution

Manganese (Mn), barium (Ba) and aluminum are used as metal precursors in the form of nitrate manganese (Mn (NO ₃ ) ₂ .6H ₂ O), barium nitrate (Ba (NO ₃ ) ₂ ) NO ₃ ) ₃ .9H ₂ O) reagents were used. Manganese / aluminum / barium, the component ratio of the high temperature oxidation catalyst, was dissolved in distilled water at a molar ratio of 1/10/1.

2. Manufacturing of urea solution

The urea solution is also prepared by stirring in distilled water. The concentration of the urea solution is about 12 times the concentration of the metal precursor.

3. Mix

The metal precursor solution and the urea solution of the same volume prepared above are mixed in a synthesis reactor to form a mixed solution. The mixed solution is stirred well evenly.

4. Precipitation reaction

The temperature of the synthesis reactor is raised to about 95 占 폚, and the mixed solution is maintained with stirring for 24 hours or more.

5. Filtration

The filtration process is carried out in order to remove the ammonium nitrate remaining in the precipitate slurry precipitated by the uniform solution precipitation method and impurities and water which are a small amount of unreacted elements and metal precursors. A filter is installed in the Buchner funnel, and the slurry of precipitate is put into the filter slurry and the waste liquid separated by the filter. The waste liquid can then be recycled into the urea solution by adding an element to be reused (the metal precursor concentration is 1 M, the element is also added to 1 M).

6. Washing

After the waste liquid is separated, ammonium nitrate remaining in the slurry slurry is removed by passing a small amount of distilled water through the slurry. The waste liquid generated here can also be stored and then put into the water washing process when the high-temperature oxidation catalyst is produced.

7. Drying and plasticity

The drying process is carried out in a drying oven at about 100 DEG C for about 10 hours or more in order to completely remove the moisture remaining in the slurry of the precipitate from which impurities and water have been removed. Thereafter, the dried precipitate slurry is heated to 1,200 ° C at a rate of about 3 ° C / min to maintain the final product for about 6 hours.

The high temperature oxidation catalyst serves to cause the oxidation reaction of the fuel gas and the decomposition / oxidation reaction of the harmful gas simultaneously. In particular, oxidation and decomposition reactions occur simultaneously at the sites corresponding to the active sites of the high-temperature oxidation catalyst. This reaction is a strong exothermic reaction, and thus a large amount of heat is generated. For example, when the toxic gas is toluene, heat of about 9,665 kcal is generated when an amount of 1 kg is treated in the high-temperature oxidation catalyst. Further, when the fuel gas is LNG, about 10,200 kcal of heat is also generated when the amount of ¹ Nm ³ is oxidized in the high temperature oxidation catalyst. This is because the fuel gas and the harmful gas are simultaneously treated in the high-temperature oxidation catalyst, and the heat quantity is equal to the heat quantity of the fuel gas and the harmful gas. Therefore, the higher the concentration of the noxious gas, the less the amount of the fuel gas is injected, so that the fuel can be saved.

The optimum condition for increasing the catalytic efficiency in the oxidation catalyst module 140 is that the space velocity (GHSV) of the mixed gas with respect to the oxidation catalyst module is 1,000 to 30,000 h ^-1 , the volume of the oxidation catalyst module 140 The density of the high temperature oxidation catalyst 141 is 0.5 to 1 g / ml, the porosity of the high temperature oxidation catalyst 141 (the ratio of the space volume to the total volume of the high temperature oxidation catalyst) is 0.3 to 0.5% . Accordingly, the pressure drop rate on the discharge side of the oxidation catalyst module 140 can be maintained within 20%.

Table 1 below is a comparative measurement of the THC concentration before and after the treatment gas passed through the oxidation catalyst module.

Number of measurements THC concentration before passage
(ppm) THC concentration after passage
(ppm) Treatment efficiency
(%) One 453 1.37 99.7 2 333 1.37 99.6 3 334 1.67 99.5 4 850 2.02 99.8 5 350 0.5 99.9 6 380 1.55 99.6

Here, the fuel gas is methane, and the harmful gas is VOC _S Type THC (total hydro-carbon) was used. Table 1 shows that the average efficiency of THC treatment is more than 99.5%, which is much better than the conventional air purification system (RTO system, activated carbon adsorption treatment system).

Table 2 below compares the existing combustion catalyst with the high temperature oxidation catalyst according to the present invention. In the treatment efficiency part, the present invention is superior to the conventional treatment system, and the operation temperature is higher than that of the conventional combustion catalyst This is possible. Therefore, it is advantageous in poisoning of tar, fine dust, sulfur compounds and chlorine compounds, and it is also advantageous in that the maintenance cost is low since a low-temperature transition metal-based high temperature combustion catalyst is used.

division Conventional combustion catalyst The high temperature oxidation catalyst Remarks Treatment efficiency 95% or more 99% or more Processing efficiency better than RTO system Operating temperature Below 400 ℃ 500 ~ 1,300 ℃ Use of high-temperature oxidation catalyst enables treatment of harmful gas at high temperature Tar, fine dust weak No problem No problem at over 500 ℃
(High temperature oxidation treatment by high temperature oxidation catalyst) Sulfur compound
(SO ₂ , H ₂ S, etc.) weak No problem No catalyst poisoning at operating conditions above 350 ℃ NO _X , CO impact No problem No problem The characteristics of the high-temperature oxidation combustion according to the present invention
: Full combustion less than 1,000 ℃ Chlorine compound weak No problem No catalyst poisoning at operating conditions above 350 ℃ Equipment cost high price
(Precious metal catalyst) low price
(Transition metal catalyst) Catalyst materials used as active sites are inexpensive transition metals and can be mass-produced, so the catalysts are generally produced at low cost

The atmospheric purification apparatus 100 according to the present invention is interposed between the gas inflow module 120 and the oxidation catalyst module 140 to mix the primary mixed gas by the primary mixing member 130 again May further include a secondary mixing member (180). In this embodiment, the secondary mixing member 180 may be in the form of a mesh.

The internal preheating heater 150 is installed in the oxidation catalyst module 140 so as to be in contact with the oxidation catalyst to provide a heat source to the oxidation catalyst 141 to activate the oxidation catalyst function.

Here, the internal preheating heater 150 may be an electric heater or an explosion-proof heater (known in the art and thus not described in detail). Unlike the conventional combustion catalyst system, the electric heater supplies the heater heat to the oxidation catalyst 141 to treat the harmful gas by the radiant heat of the catalyst, thereby oxidizing the oxidation catalyst in a flameless manner. In this case, since it is a flameless method, the risk of fire or explosion can be excluded, and since the catalyst is not combusted, the lifetime of the catalyst can be prolonged, so that the catalyst consumption can be significantly reduced compared with the combustion type, .

In addition, the present invention may further include an external preheater 190 that surrounds the oxidation catalyst module 140 and further activates the oxidation catalyst function by providing a heat source to the oxidation catalyst 141.

The external preheater 190 may be applied, for example, in such a form that it is divided into two parts and assembled annularly by the clamp 191, but the present invention is not limited thereto.

The connecting chamber module 160 is stacked on the oxidation catalyst module 140 to induce a high temperature oxidizing gas from the oxidation catalyst module. In particular, the connecting chamber module 160 includes an external preheater 190, It is difficult to connect the oxidation catalyst module to the exhaust stack 170 structurally. Therefore, it is a complementary structure for indirectly connecting the oxidation catalyst module and the exhaust stack.

The exhaust stack 170 is provided to communicate with the inside of the connecting chamber module 160 and discharges the oxidizing gas in the connecting chamber module to the outside. The upper and lower portions are divided and flanged Shape can be provided.

The waste heat recovery module 210, 3h, which is installed in the connection stack 200 connecting the connecting chamber module 160 and the exhaust stack 170, recovers waste heat from the hot oxidizing gas passing through the connection stack, 3). ≪ / RTI >

The waste heat recovery module 210 is constructed such that the connection stack 200 is divided into a first connection stack 201 provided on the oxidation catalyst module 140 side and a second connection stack 202 provided on the exhaust stack 170 side And can be flanged between the first and second connection stacks 201 and 202. [

The waste heat recovery module 210 includes a plurality of heat exchange pipes 211 communicating with the first and second connection stacks 201 and 202 through which high temperature oxidizing gas passes and first and second connection stacks 201 and 202, And a waste heat recovery tank 212 filled with a coolant 213 for cooling the heat exchange pipe.

The waste heat recovery cylinder 212 may be provided with a refrigerant inlet 212a for introducing the refrigerant and a refrigerant outlet 212b for discharging the refrigerant. Accordingly, the hot oxidizing gas passing through the heat exchanging pipe 211 is cooled while being exchanged by the refrigerant. In this process, the refrigerant is heated at a high temperature by the heat exchanging action, so that it is recovered through the refrigerant discharging port 212b, Since it can be utilized as a heat source, energy can be utilized efficiently.

In addition, the inner surface of the waste heat recovery tank 212 of the waste heat recovery module 212 is preferably coated with an anti-pollution coating agent to prevent contamination.

Wherein the coating agent comprises 20 to 30 wt% of polyol, 15 to 20 wt% of at least one functional alcohol selected from fluoroalcohol or silanol, 15 to 25 wt% of isocyanate, 5 to 8 wt% of blocking agent, 20 to 40 wt% 3 to 10% by weight of an amine monomer, 1 to 3% by weight of an additive and 1 to 3% by weight of an organometallic catalyst.

The polyol is added to impart a function such as tensile strength, tear strength, abrasion resistance, etc. to the composition. Preferably, the polyol is at least one selected from the group consisting of polyethylene glycol, polypropylene glycol, polybutylene glycol and polyisoprene glycol You can choose. At this time, when the polyol is contained in an amount of less than 20% by weight based on the total weight of the composition, workability due to an increase in the viscosity of the composition is deteriorated. When the polyol is contained in an amount exceeding 30% by weight, mechanical properties of the coating film formed by curing It may cause deterioration of workability and film strength, so that it is preferable to be included in the range of 20 to 30% by weight. In one embodiment of the present invention, the polyol was a mixture of PP-3000 and GP-4000 manufactured by KPX Chemicals.

The functional alcohol is at least one alcohol selected from fluoroalcohol or silanol, and is added to impart abrasion resistance, weather resistance, and stain resistance to the polyurea composition. Therefore, by including the functional alcohol, not only the flame retardancy is imparted to the composition but also the mechanical properties such as heat resistance, cold resistance, weather resistance, and aging resistance can be remarkably improved.

Among the functional alcohols, the fluoroalcohol is a compound having a structure in which OH is bonded to the end of a fluoroalkyl group (CnF _{2n + 1} ), and specific examples thereof include 2,2,2-trifluoroethanol, 2,2,3,3- Tetrafluoro-1-propanol, 2,2,3,3,3-pentafluoro-1-propanol, 2,2,3,4,4,4-hexafluoro-1-butanol, 2,2,3,3 , 4,4,4-heptafluor-1-butanol, 2,2,3,3,4,4,5,5-octafluoro-1-pentanol, 2,2,3,3,4,4, 5,5,5-nonanfluor-1-pentanol, 2,2,3,3,4,4,5,5,6,6,7,7,8,8-pentadecafluoro-1-octanol , 4-fluoro-a-methylbenzyl alcohol can be used. The silanol in the functional alcohol may be selected from the group consisting of trimethylsilanol, triphenylsilanol, methylphenylvinylsilanol, ethylbenzylvinylsilanol, dibutylvinylsilanol, propylphenylallyl silanol, and ethylbenzylallyl silanol Or more of the silanol monomers having a purity of 80 to 100% can be used.

At this time, the functional alcohol is included in the range of 15 to 20 wt% based on the total weight of the composition. If it is contained in an amount of less than 15% by weight, the effect of imparting weatherability, stain resistance and mechanical properties required in the present invention is insignificant. When it is contained in an amount of more than 20% by weight, viscosity increases and the content of other compositions is relatively small There is a problem that it becomes difficult to obtain desired physical properties. In one embodiment of the present invention, the functional alcohols are 4-fluoro-a-methylbenzyl alcohol having a purity of 98 to 100% by Aldrich or trimethylsilanol having a purity of 80 to 100%, either singly or in combination.

In the present invention, the isocyanate may be at least one selected from the group consisting of hexamethylene diisocyanate trimer (HDT), isophorone diisocyanate (IPDI), cyclohexylmethane diisocyanate (H12MDI), methylene diphenyl isocyanate Diisocyanate, MDI), and toluene diisocyanate (TDI). At this time, the higher the isocyanate or NCO content, the higher the hardness or the difficulty in controlling the reaction, so that the NCO content of the isocyanate is preferably 5 to 10%. If the amount of the isocyanate is less than 15% by weight, the viscosity of the composition increases and the mechanical properties of the composition deteriorate. When the amount of the isocyanate exceeds 25% by weight, The viscosity of the composition is lowered, the adhesive strength is lowered, and the hardness is increased, which is undesirable.

The present invention also provides an adsorption module 220 disposed between the connecting chamber module 160 and the exhaust stack 170 and serving as a kind of filter packed with an adsorbent material for adsorbing toxic substances contained in the oxidizing gas . Since the adsorption module 220 is also flanged, it is easy to disassemble and combine as needed.

In this atmosphere purifying apparatus 100, noxious gas components such as CO and NO _x are 7 ppm and 0.1 ppm, respectively, among the components of the exhaust gas discharged through the exhaust stack 170, and almost no noxious gas components are generated. In particular, in the case of NO _x , it is close to zero. In view of this, the atmospheric purification apparatus 100 according to the present invention shows excellent efficacy in purifying polluted air.

Next, the explosion-proof atmosphere purifying system 300 will be described.

FIG. 4 is a configuration diagram of an air purifying system according to the present invention, which is a state diagram at the time of normal operation, FIG. 5 is a configuration diagram of an air purifying system according to the present invention, FIG. 2 is a block diagram of an air purifying system according to the present invention. FIG.

As shown in Figs. 4 to 6, the air purifying system 300 has a configuration in which a safeguard device is added to the air purifying device 100 to allow the air purifying device to operate safely.

The air purifying system 300 includes an air purifying device 100. In addition, when the internal temperature of the oxidation catalyst module 140 is higher than a set temperature, the cooling air is supplied to the interior of the gas inflow module 120, A primary cooling means (310) for discharging the cooled air to the oxidation catalyst module (140) or the exhaust stack (170); When the internal temperature of the oxidation catalyst module 140 is higher than the set temperature due to the cooling action by the primary cooling means, the cooling air is supplied to the connecting chamber module 160, and the supplied cooling air is supplied to the exhaust stack 170 And a secondary cooling means 320 for discharging the cooling water.

The primary cooling unit 310 includes a first cooling fan 311 operated when the internal temperature of the oxidation catalyst module 140 is higher than the set temperature, A first cooling air supply line 312 connecting the first cooling fan and the gas inflow module to supply the first cooling air to the inside of the first cooling air supply line, a first supply valve 313 selectively opening and closing the first cooling air supply line, A first cooling air exhaust line 314 connecting between the gas inflow module and the exhaust stack for discharging the cooling air supplied to the inside of the gas inflow module 120 to the exhaust stack 170, And a first exhaust valve 315 for selectively opening the exhaust valve 315.

The secondary cooling means 320 includes a second cooling fan 321 that is operated when the internal temperature of the oxidation catalyst module is higher than the set temperature by the operation of the primary cooling means 310, A second cooling air supply line 322 connecting between the second cooling fan and the connecting chamber module to supply the cooling air to the interior of the connecting chamber module 160, A valve 323 and a second cooling air exhaust line 324 connecting between the connecting chamber module and the exhaust stack for discharging the cooling air supplied into the connecting chamber module to the exhaust stack 170 .

The first pressure regulating means 330 regulates the supply pressure of the noxious gas supplied to the interior of the air purifying device 300 to a constant level. And may further comprise adjustment means 340.

The first pressure regulating means 330 is installed on the noxious gas supply line 301 to regulate the air pressure of the noxious gas supplied to the gas inflow module 120 of the air purifier 100 A pressure regulating valve 331 and a first bypass line 332 for bypassing an overpressure higher than a set pressure of air pressure of the supplied noxious gas to the exhaust stack 170.

The second pressure regulating means 340 includes a connecting line 341 connecting between the gas inflow module 120 and the exhaust stack 170 of the air purifying device 100, And a second pressure regulating valve 342 for discharging the overpressure more than the set pressure to the exhaust stack 170 when the pressure is higher than the set pressure.

Reference numeral 350 denotes a harmful gas bypass line for bypassing the noxious gas to the exhaust stack 170; and 360, a bypass line open / close valve for selectively opening and closing the noxious gas bypass line.

4, when the air purifier 100 operates normally without overheating or overpressure, harmful components are removed while the noxious gas passes from the lower portion to the upper portion of the air purifier 100 The clean gas is discharged to the outside through the exhaust stack 170.

5 is a primary safety mode in which overheat occurs in the oxidation catalyst module 140 and is operated when the internal temperature of the oxidation catalyst module 140 is higher than the set temperature. In the primary safety mode, The first cooling fan 311 of the cooling means 310 is operated and the cooling air blown from the first cooling fan is supplied to the inside of the gas inflow module 120 through the first cooling air supply line 312. The cooling air thus supplied flows to the upper portion of the air purifier 100 to cool the oxidation catalyst module 140.

In the case of FIG. 6, the secondary safety mode is activated when the temperature in the oxidation catalyst module 140 is still higher than the set temperature despite the primary cooling by the primary cooling means 310, The cooling air in the gas inflow module 120 is discharged directly to the exhaust stack 170 through the first cooling air exhaust line 312 and at the same time the secondary cooling means is operated.

The second cooling fan 320 operates the second cooling fan 321 and the cooling air blown from the second cooling fan is supplied to the inside of the connecting chamber module 160 through the second cooling air supply line 322 And the cooling air supplied to the connecting chamber module is discharged directly to the exhaust stack 170 through the second cooling air exhaust line 324. [

The operation of the internal preheater 150 and the external preheater 190 is stopped and the noxious gas is discharged directly to the exhaust stack 170 through the noxious gas bypass line without flowing into the air purification apparatus 100 .

The first valve 313, the first exhaust valve 315, the second supply valve 323, the bypass line on-off valve 360, and the noxious gas line valve 370 are automatically It is preferable that an automatic opening / closing valve for opening / In addition, it is preferable that the manual valve 380 is installed in parallel with the automatic open / close valve 380 in consideration of when the automatic open / close valve becomes inoperable due to a failure.

While the present invention has been particularly shown and described with reference to embodiments thereof, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the invention.

100: atmospheric purification apparatus 110: frame
120: gas inlet module 130: primary mixing member
140: Oxidation catalyst module 150: Internal preheating heater
160: connecting chamber module 170: exhaust stack
180: secondary mixing member 190: external preheating heater
200: connection stack 210: waste heat recovery module
220: Adsorption module 300: Atmospheric purification system
310: primary cooling means 320: secondary cooling means
330: first pressure regulating means 340: second pressure regulating means

Claims (22)

frame;
A gas inlet module fixed to the frame and having a first inlet port through which fuel gas and air are introduced and a second inlet port through which fuel gas and noxious gas are introduced;
A primary mixing member provided at an inner upper portion of the gas inlet module to mix gases raised from the gas inlet module;
An oxidation catalyst module which is stacked to communicate with the gas inflow module and is filled with an oxidation catalyst for decomposing noxious gas by radiant heat due to oxidation catalysis;
An internal preheating heater installed inside the oxidation catalyst module so as to be in contact with the oxidation catalyst to provide a heat source to the oxidation catalyst to activate oxidation catalyst operation;
A connecting chamber module which is stacked so as to communicate with the oxidation catalyst module and into which high temperature oxidizing gas flows from the oxidation catalyst module; And
And an exhaust stack provided in communication with the inside of the connecting chamber module for discharging the oxidizing gas in the connecting chamber module to the outside.
The method according to claim 1,
Further comprising a secondary mixing member interposed between the gas inlet module and the oxidation catalyst module to mix the primary mixed gas again by the primary mixing member, wherein the secondary mixing member has a shape of a mesh Flameless air purification system using high temperature oxidation catalyst.
The method according to claim 1,
And an external preheater for surrounding the outside of the oxidation catalyst module and providing an oxidizing catalyst with a heat source to activate an oxidation catalyst function.
The method according to claim 1,
Further comprising a waste heat recovery module installed in a connection stack connecting the connecting chamber module and the exhaust stack, the waste heat recovery module recovering waste heat from the hot oxidizing gas passing through the connection stack.
The method of claim 4,
The connection stack includes a first connection stack on the oxidation catalyst module side and a second connection stack on the exhaust stack side,
The waste heat recovery module includes: a plurality of heat exchange pipes communicating with the first and second connection stacks to pass hot oxidizing gas; A heat exchanging pipe, a flange joined between the first and second connection stacks, a refrigerant for cooling the heat exchange pipe is filled therein, a refrigerant inlet for introducing the refrigerant and a refrigerant outlet for discharging the refrigerant, Flame-type air purification apparatus using a high-temperature oxidation catalyst composed of a flue-type flue gasifier.
The method according to claim 1,
The internal preheating heater is a flame-type air purification apparatus using a high-temperature oxidation catalyst, which is either an electric heater or an explosion-proof heater.
The method according to claim 1,
Each module is a flameless air purification unit utilizing a high temperature oxidation catalyst coupled by flange joints.
The method according to claim 1,
And an adsorption module disposed between the connecting chamber module and the exhaust stack and filled with an adsorbent material for adsorbing harmful substances contained in the oxidizing gas.
The method according to claim 1,
The oxidation catalyst is a flame-type air purification apparatus using a high-temperature oxidation catalyst which is a hexaaluminate-based catalyst having a transition metal.
The method of claim 9,
Wherein the transition metal component comprises a high temperature oxidation catalyst comprising at least one of manganese, cobalt, iron or chromium.
The method according to claim 1,
Wherein the oxidation catalyst comprises a high temperature oxidation catalyst containing nitrate transition metal, alkaline earth metal and aluminum nitrate, wherein the alkaline earth metal comprises at least one of calcium, strontium, barium or radium.
The method of claim 11,
Wherein the molar ratio of nitrate transition metal / alkaline earth metal / aluminum nitrate is (1-x) / (1-y) / 11, x is a number in the range of 0.1 to 0.5 and y is a number in the range of 0.1 to 0.5. A flame-type air purification apparatus using a flame-type air purification apparatus.
The method according to claim 1,
A flame-type air purification apparatus using a high-temperature oxidation catalyst in which the amount of CO (carbon monoxide) discharged from the oxidation catalyst module is 20 ppm or less.
The method according to claim 1,
NO _x emitted from the oxidation catalyst module A flame-based air purification apparatus using a high-temperature oxidation catalyst having an amount of 20 ppm or less.
The method according to claim 1,
Flame-based air purification system using high-temperature oxidation catalyst with 99% or more treatment efficiency of harmful gas.
16. The method of claim 15,
The harmful gas is a flame-type air purification apparatus using a high-temperature oxidation catalyst including a volatile organic compound type including petroleum gas, a sulfur compound type, an ammonia compound, and a halogen compound.
A flame-based air purification apparatus using the high-temperature oxidation catalyst according to any one of claims 1 to 16,
A primary cooling means for supplying cooling air to the interior of the gas inflow module when the internal temperature of the oxidation catalyst module is higher than the set temperature and for allowing the supplied cooling air to be discharged to the oxidation catalyst module or the exhaust stack; And
A secondary cooling means for supplying the cooling air to the connecting chamber module and discharging the supplied cooling air to the exhaust stack when the internal temperature of the oxidation catalyst module is higher than the set temperature even by the cooling action by the primary cooling means Further comprising an explosion-proof atmospheric purification system.
18. The method of claim 17,
The primary cooling means,
A first cooling fan operated when the internal temperature of the oxidation catalyst module is higher than the set temperature;
A first cooling air supply line connecting between the first cooling fan and the gas inflow module to supply the cooling air of the first cooling fan to the inside of the gas inflow module;
A first supply valve for selectively opening and closing the first cooling air supply line;
A first cooling air exhaust line connecting between the gas inlet module and the exhaust stack to exhaust the cooling air supplied to the interior of the gas inlet module to the exhaust stack; And
And a first exhaust valve for selectively opening the first cooling air exhaust line.
18. The method of claim 17,
The secondary cooling means,
A second cooling fan operated when the internal temperature of the oxidation catalyst module is higher than the set temperature by the operation of the primary cooling means;
A second cooling air supply line connecting between the second cooling fan and the connecting chamber module for supplying the cooling air of the second cooling fan to the inside of the connecting chamber module;
A second supply valve for selectively opening and closing the second cooling air supply line; And
And a second cooling air exhaust line connecting between the connecting chamber module and the exhaust stack for discharging the cooling air supplied to the inside of the connecting chamber module to the exhaust stack.
18. The method of claim 17,
A first pressure regulating means for regulating a supply pressure of the noxious gas supplied to the inside of the atmospheric purifier uniformly; And
And second pressure regulating means for regulating a pressure inside the air purifying device to a constant level.
The method of claim 20,
The first pressure regulating means
A first pressure regulating valve installed on the noxious gas supply line for regulating the air pressure of the noxious gas supplied to the gas inflow module of the atmospheric purifier uniformly; And a first bypass line for bypassing an overpressure higher than a set pressure in the air pressure of the supplied noxious gas to the exhaust stack,
The second pressure regulating means
A connection line connecting the gas inlet module of the air purification apparatus and the exhaust stack; And a second pressure regulating valve installed on the connecting line for discharging an overpressure exceeding the set pressure to the exhaust stack when the internal pressure of the gas inflowing module is higher than the set pressure.
18. The method of claim 17,
A harmful gas bypass line for bypassing the noxious gas flowing into the noxious gas supply line to the exhaust stack;
And a bypass line open / close valve for selectively opening and closing the harmful gas bypass line.

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