KR200359604Y1 - Catalytic oxidation adsorption tower - Google Patents

Abstract

The present invention relates to a catalytic oxidation adsorption tower, and more particularly, by completely oxidatively decomposing a contaminated gas using a catalytic oxidation adsorbent installed therein, it does not discharge secondary pollutants, and regenerates the catalytic oxidation adsorbent itself. The present invention relates to a catalytic oxidation adsorption tower that minimizes the generation of secondary waste.

Since the catalytic oxidation adsorption tower according to the present invention has a parallel adsorption structure, the operation of the production equipment can be utilized 100%, and the second generation waste cost can be minimized since the catalytic oxidation adsorbent with reduced function is used again and again. In addition, the operating cost is reduced.

Description

Catalytic oxidation adsorption tower

The present invention relates to a catalytic oxidation adsorption tower, and more particularly, by completely oxidatively decomposing a contaminated gas using a catalytic oxidation adsorbent installed therein, it does not discharge secondary pollutants, and regenerates the catalytic oxidation adsorbent itself. The present invention relates to a catalytic oxidation adsorption tower that minimizes the generation of secondary waste.

Volatile Organic Compounds (hereinafter referred to as VOCs) refer to petrochemical products with a vapor pressure of more than 10.3 kilo Pascals (or 1.5 psia) in hydrocarbons. It is defined as a substance announced in consultation with the Chairman (Article 39 (1) of the Enforcement Decree of the Atmospheric Environment Conservation Act), and in the US EPA, "VOCs are photochemically oxidized with NOx by sunlight in the atmosphere. Organic compounds that cause smog by increasing ozone concentration.

When looking at the characteristics of VOCs, there are a number of examples, but the representative substance itself is harmful to the human body (aromatic hydrocarbons: benzene, toluene, xylene, etc., halogen hydrocarbons: hydrocarbons containing Cl, F), and ozone generation near the surface Is contributing indirectly to global warming. In addition, when exposed to high concentrations of VOCs anesthesia (inhibits the central nervous system), dizziness, paralysis and death cause acute disorders, specific toxicity of each material is shown in Table 1, ozone production is shown in Table 2.

matter Health disorder benzene Hematopoietic dysfunction (cytopenia, aplastic anemia), arrhythmia, carcinogenicity (leukemia) Halogenated hydrocarbons Hepatotoxicity, renal toxicity, cardiotoxicity (arrhythmia, sudden death), carcinogenicity in animals Methanol Blindness, metabolic acidosis Formaldehyde Allergic dermatitis, reduced lung function, carcinogenicity in animals Normal hexane Peripheral Nerve Disorder

Atmospheric Chemical Reactions of VOCs Remarks The most important role of VOCs in the atmosphere is the presence of NOx, which reacts with OH radicals and generates ozone, causing photochemical oxidants.VOC + 2NO + 2O2 → H2O + 2NO2 + R'C (O ) R "NO2 + hv → NO + OO + O2 + M → O3 + M Therefore, VOC + 3O2 → H2O + O3 + R'C (O) R" VOCs present with NOx cause ozone

Since 1980, the modern society has been trying to improve the welfare of the people and increase the income due to the rapid development of the industry, but has emitted pollutants such as odors and VOCs from various raw materials and wastes which are by-products of the industrial economy. In 1996, during the process of petroleum refining and petrochemical products at Yeocheon Petrochemical Complex, VOCs were released during the process, causing large complaints such as complaints of odor pollution from residents, and in 1997, most of the causes of odor complaints in Sihwa area were It is estimated to be due to emissions.

Therefore, it is natural that the VOCs are treated before being discharged to the atmosphere, and the treatment methods of the VOCs are broadly divided into a method of recovering / reusing VOC materials and a method of decomposing the VOCs. That is, when the discharged VOC is discharged at a relatively high concentration from a single outlet and economical (that is, when the recovery cost is less than the purchase cost), it is preferable to install a recovery facility. Carbon adsorption), scrubbing and cryogenic condensation. On the other hand, if the VOCs are not a single substance but a mixture or harmful substance, or if there is no recovery value, it is preferable to install a decomposition facility rather than a recovery facility.The techniques available for decomposition include thermal oxidation, Catalytic Oxidation and Bio-Filtration. And the characteristics of each VOCs treatment method can be summarized as shown in Table 3 below.

Control technology Capital cost Operating costs Use in the actual field Process flexibility Mass processing capacity Applicability to Low Contaminants Heat Incineration Absorption Absorption Livestock Filtration Catalyst Oxidation Photocatalytic Oxidation High and low High, medium, low, low 0000 × (0) ×× 00 ×× 000 000 ×××× 00000 ××

In addition, looking at the domestic prior patents related to the deodorant, Korean Registered Patent No. 332511 discloses a malodor treatment agent by mixing rice bran with yeast, adding zeolite, kneading and fermenting, and then mixing and drying iron sulfate. Patent No. 139559 discloses activated carbon fibers and nonwoven fabrics and a method of manufacturing the same. In addition, in Korean Patent Application No. 88-017920, the mordenite-based natural zeolite is heat treated at 200 to 350 ° C., followed by acid treatment with an aqueous hydrochloric acid solution of 0.8 N or less, followed by calcium ion exchange with an aqueous calcium chloride solution of 0.7 N or less. Disclosed is a method for producing a carbon dioxide adsorbent using a natural zeolite.

However, these conventional odor and VOCs treatment methods are substantially lower in use value when applied to the site because the odor removal efficiency is significantly lower, the initial construction cost is high, the secondary waste is generated, and the operating cost is also uneconomical. It has a disadvantage.

That is, in the case of activated carbon, which has the property of adsorbing other components even though water is present, and which has a relatively high molecular weight and high resistance to components that are not hydrophilic (hydrophobic components), the usage amount is the most widely used. For gas containing soot or dust, pretreatment is required, and the problem of high concentration of odor is that the service life of the adsorbent is shortened due to the limitation of adsorption capacity. In addition, maintenance costs are increased due to the situation that the supply of activated carbon is completely 100% imported and secondary pollutants generated during regeneration of used adsorbent, and smooth periodic replacement is essential to maintain adsorbent performance. There are also disadvantages.

In addition, in the case of a thermal incinerator, the operation cost is relatively high due to the cost of the auxiliary fuel, the gas flow rate is increased, and the residence time is shortened, and the combustion gas is incompletely combusted when the mixing of the combustion gas is not performed. In addition, the increased gas flow rate lowers the combustion chamber temperature, lowering the treatment efficiency and is generally not cost effective for treating low concentration VOCs.

Catalytic incinerators also require less fuel and can be operated at lower temperatures. However, waste catalysts that require high initial costs, catalyst poisons and sometimes dust removal and non-recyclable waste must be treated as designated wastes. have.

If these incompletely installed or unprocessed odors and harmful gases spread around, they will return to us as environmental disasters that not only destroy the natural environment but also threaten humanity.

On the other hand, when odors or VOCs are generally treated by adsorption, carriers such as activated carbon and zeolites are used as adsorbents, but side effects such as waste generation due to secondary pollution are very low. . Existing activated carbon has almost no resources in Korea, such as coconut shell charcoal, palm shell charcoal, lignite charcoal, charcoal and ash, anthracite charcoal and petroleum coke, and imports 100% raw materials to process or import finished products to activate activated carbon. Was prepared and produced (Smisek and cerny, 1970). Imports of such raw materials waste foreign currency and are not considered to be desirable to enhance national competitiveness. In addition, gas (water vapor, carbon dioxide, etc.) and pickling generated by oxidation of carbon in the temperature range of 800-1000 ° C during the manufacturing process Chemicals in the process (inorganic chemicals such as zinc chloride, phosphoric acid and sulfuric acid) cause device corrosion and secondary environmental pollution, and have disadvantages such as complexity of the manufacturing process. In addition, the ability to remove VOCs from activated carbon shows that the demand for high-performance non-flammable absorbents is rapidly increasing due to the tightening of regulations on refinery oil reformers and gasoline, and the regulation of formaldehyde and organic solvents in the paint and carpet manufacturing sectors. However, although there are some differences depending on the properties of the gas, as well as a low adsorption rate of 10 to 36%, the service life (use time) is very short, it was found to be economical.

Synthetic zeolites are receiving great attention. Japanese engineering firms in this area are developing VOCs capture devices using hydrophilic synthetic zeolites that are high in silica.

Belgian chemists have developed a method for removing nitrogen oxide (NOx) from tailpipe emissions of internal combustion engines that inject excess air using zeolite to reduce fuel consumption and reduce carbon dioxide emissions [Angew. Chem. Int. Ed., 39, 2934 (2000).

Prof. Ahn Seong-yu of the University of Osaka's Department of Engineering highly disperses the titanium oxide photocatalyst with molecular structure control in zeolites with many micropores to decompose nitrogen oxides (NOx) into harmless nitrogen and oxygen. Succeeded in doing. In addition, the photocatalytic reaction of titanium oxide proceeded only in ultraviolet light, but Professor Lee succeeded in developing the second generation titanium oxide photocatalyst in which photocatalytic reaction proceeds efficiently in visible light by ion implantation of chromium and vanadium into titanium oxide. It has achieved the result of linking zeolite to full-fledged application of photocatalysts, such as expression and high activation of new functions using zeolite as a catalyst carrier, and extending the range of use of light to visible light by ion implantation (Japan Chemical Industries, 12.12. 1998).

The present invention has been made to solve the problems described above, the purpose of the catalytic oxidation is made by reversibly combining the inorganic oxidizing agents such as calcium and sodium into the synthetic zeolite which is a carrier having excellent adsorption capacity By providing an adsorbent therein, it is possible to provide a catalytic oxidation adsorption tower in which contaminated gas can be purified while passing through a catalytic oxidation adsorbent and discharged into clean air from which odors and VOCs are completely removed.

Another object of the present invention is to provide a catalytic oxidation adsorption tower capable of minimizing generation of secondary wastes by regenerating a catalytic oxidation adsorbent installed therein.

The catalytic oxidation adsorption tower according to the present invention for achieving the above object is formed in the lower portion of the inlet is formed with the inlet of the contaminated gas, the upper portion is formed with the exhaust port is discharged, the space between the inlet and the exhaust opening An adsorption tower structure in which the partition is divided into a first space part and a second space part in parallel, an upper part of the first and second space parts is closed by an upper partition, and a lower part is closed by a lower partition; First and second catalyst oxidizing adsorbents, each of which is installed at least one of the first and second space parts to oxidatively adsorb contaminants; Chemical injection means for spraying the regeneration solution only on the catalytic oxidation adsorbent which requires regeneration due to deterioration of the function of the first and second catalyst oxidation adsorbents; Heater means for heating and drying only the catalytic oxidation adsorbent sprayed with the regeneration solution; And a first valve at a position corresponding to the first space part, and a second valve at a position corresponding to the second space part, which are installed at the upper partition and the lower partition, and separate the first valve and the second valve. It comprises a valve means for selectively on / off through the control unit.

Here, the catalytic oxidation adsorbent is characterized in that the inorganic oxidizing agent is ion-implanted into the synthetic zeolite as a carrier and reversibly combined.

In addition, the chemical injection means is a chemical tank in which the regeneration solution is stored, a transfer pipe connected to the chemical tank to transfer the regeneration solution, a plurality of distribution pipes connected to the end of the delivery pipe to distribute the regeneration solution, and the first catalyst A first chemical injection nozzle installed in the distribution pipe to inject the regeneration solution from the upper portion of the oxidizing adsorbent, a second chemical injection nozzle installed in the distribution pipe to spray the regeneration solution into the upper portion of the second catalyst oxidizing adsorbent; And a pump which is installed at a part of the transfer pipe forcibly transferring the regeneration liquid of the chemical tank to the chemical injection nozzle, and a chemical injection control unit for controlling on / off of the first and second chemical injection nozzles, operation of the pump and injection time. It is configured to include.

In addition, the heater means selectively operates the first heater installed under the first catalyst oxidizing adsorbent, the second heater provided under the second catalyst oxidizing adsorbent, and the first and second heaters, The heater control part which controls the temperature and heating time is comprised.

1 is a cross-sectional view schematically showing the configuration of a catalytic oxidation adsorption tower according to the present invention,

Figure 2 is a flow chart sequentially showing a process for removing odor and volatile organic compounds using the catalytic oxidation adsorption tower according to the present invention.

◎ Explanation of symbols for main part of drawing

100: adsorption tower structure 102: injection hole

104: exhaust port 110: partition wall

120: first space portion 130: second space portion

140: upper partition 150: lower partition

200: duct 210: hood

220: fan 300: valve control unit

310: first valve 320: second valve

410: first catalyst oxidized adsorbent 420: second catalyst oxidized adsorbent

500: chemical injection control unit 510: chemical tank

520: transfer pipe 530: distribution pipe

540: first drug injection nozzle 550: second drug injection nozzle

560: pump 600: heater control unit

610: first heater 620: second heater

Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

1 is a cross-sectional view schematically showing the configuration of the catalytic oxidation adsorption tower according to the present invention.

Referring to this, the present invention has an adsorption tower structure (100) formed with an inlet (102) through which contaminated gas is introduced into a lower portion, and an exhaust (104) through which gas is discharged. In the adsorption tower structure 100, a space between the inlet 102 and the exhaust port 104 is divided by the partition wall 110 and the first space 120 and the second space 130 are arranged in parallel. To be prepared. In addition, an upper portion of the first and second space portions 120 and 130 is sealed by the upper partition 140, and a lower portion thereof is sealed by the lower partition 150. Therefore, a storage space of the contaminated gas introduced through the injection hole 102 is provided between the lower partition 150 and the bottom surface.

And the upper partition 140 and the lower partition 150 is provided with a valve means, the valve means is a plurality of first valve 310 provided in the upper partition and the lower partition corresponding to the first space portion 120, It is divided into a plurality of second valves 320 provided in the upper partition and the lower partition corresponding to the second space portion 130. In addition, the first valve 310 and the second valve 320 are opened and closed by a separate valve control unit 300.

And the inlet 102 of the adsorption tower structure 100 is installed in communication with the duct 200 for transferring the contaminated gas, the end of the duct 200 is provided with a hood 210, a portion of the duct 200 A fan 220 is provided to suck the contaminated gas through the hood 210 and force it to the injection hole 102.

Herein, polluted gas refers to chemical gases and volatile organic compounds that are contained in the odor generated in everyday life, the storage of various petroleum products and volatile liquid substances, loading, unloading, and discharged from the processes of the synthetic organic compound manufacturing facility. Refers to substances (Volatile Organic Compounds, hereinafter VOCs).

Next, each space portion is provided with at least one catalytic oxidation adsorbent is configured to oxidatively adsorb contaminants. That is, three to five first catalyst oxidizing adsorbents 410 are installed in the first space portion 120 at predetermined intervals along the length direction, and the second space portion 130 is provided along the length direction. About 3 to 5 second catalytic oxidation adsorbents 420 are provided at intervals of.

Here, the catalytic oxidation adsorbent is made by reversibly combining inorganic oxidizing agents such as manganese, calcium, and sodium with synthetic zeolite, which is a carrier having excellent adsorption capacity, and refer to Korean Patent Application No. 2003-40278 of the applicant. .

Next, chemical injection means for supplying regeneration solution to each catalytic oxidation adsorbent and heater means for drying each catalytic oxidation adsorbent are provided.

The chemical injection means is installed in parallel with the adsorbent structure 100, the chemical tank 510 to store the regeneration solution, the transfer pipe 520 is connected to the chemical tank to transfer the regeneration solution, and connected to the end of the delivery pipe And a distribution pipe 530 provided to distribute the transferred chemicals to the respective catalytic oxidation adsorbents, and a pump provided in a portion of the delivery pipe 520 to force the chemicals stored in the chemical tank 510 to the distribution pipe 530. 560, the first and second chemical injection nozzles 540 and 550 provided in respective distribution pipes, and the first chemical injection nozzle 540 and the second chemical injection nozzle 550 are selectively turned on / off. The chemical injection control unit 500 is turned off.

Here, the nozzle for injecting the regeneration solution into the first catalyst oxidizing adsorbent 410 is called the first chemical injection nozzle 540, and the nozzle for injecting the regeneration solution into the second catalyst oxidizing adsorbent 420 is called the second chemical injection nozzle. It is called (550). And the chemical injection control unit 500 is to control the injection time as well as whether the nozzle opening and closing.

In addition, the regeneration liquid (oxidant) used in the present invention refers to a known inorganic oxidation deodorant, and any one can be used as long as the pollutant adsorbed on the catalytic oxidation adsorbent is separated by oxidation. The injection amount is preferably 15 L / hr, the regeneration interval is 2 times / day, and the concentration is kept at 0.5%.

For reference, the regeneration method of the catalytic oxidation adsorbent is shown in Table 4 below.

division Way Remarks Zeolite form Zeolite particle size How to play Playback interval Regenerative saline Brine concentration (%) Regeneration flow rate (L / hr) Duration (hr) Playback pH Regeneration Efficiency (%) Zeolite-Na type 3 * 6, 4 * 8 Upflow 2 times / day Inorganic Oxidative Deodorant 0.5 15 1.5 12 95 -Once a year -After changing the adsorbent, transform it into powder and reuse it as wastewater treatment chemicals.

The heater means is divided into a first heater 610 installed under each of the first catalytic oxidation adsorbents 410, and a second heater 620 installed under each of the second catalytic oxidation adsorbents 420, The first heater 610 and the second heater 620 are selectively operated through a separate heater controller 600 to dry the catalytic oxidation adsorbent.

Now, the operation of the catalytic oxidation adsorption tower according to the present invention configured as described above and a method of removing odor and volatile organic compounds using the same will be described with reference to the flowchart of FIG. 2.

First, the contaminated gas containing malodor and volatile organic compounds is introduced into the adsorption tower structure 100 using the hood 210 and the duct 200 (S10). In this case, when only the first valve 310 is opened through the valve control unit 300, the gas introduced into the adsorption tower structure 100 is discharged to the exhaust port 104 through the first space part 120. Of course, when the contaminated gas passes through the first space part 120, it is oxidized and adsorbed while passing through the plurality of first catalyst oxidizing adsorbents 410 to completely remove the odor and volatile organic compounds by oxidative decomposition (S20). , Only clean air is discharged into the atmosphere (S30).

Next, when the adsorption oxidation function of the first catalyst oxidizing adsorbent 410 decreases after a certain period of time, the first valve 310 is closed through the valve control unit 300, and the second valve 320 is opened. Then, the contaminated gas is blocked from flowing into the first space 120, and is discharged to the exhaust port 104 through the second space 130. Of course, when passing through the second space portion 130, it is oxidized and adsorbed while passing through the plurality of second catalyst oxidizing adsorbents 420 to remove odors and volatile organic compounds, and only clean air is discharged into the atmosphere.

When the polluted gas is oxidized and adsorbed through the second catalyst oxidizing adsorbent 420, the regeneration operation of the first catalyst oxidizing adsorbent 410 is started. That is, the pump 560 is operated according to the signal of the chemical injection control unit 500 and the regeneration solution stored in the chemical tank 510 is transferred to the first chemical injection nozzle 540 through the transfer pipe 520 and the distribution pipe 530. The first chemical injection nozzle 540 is opened, and a predetermined amount of the regeneration liquid is injected into the first catalyst oxidizing adsorbent 410 (S40). Next, when the injection of the regeneration solution is completed, the first heater 610 is operated in response to a signal from the heater controller 600 to heat-dry the first catalyst oxidized adsorbent 410 into which the regeneration solution is injected. At this time, it is preferable to perform a heating operation for 2 to 3 hours at 80 to 100 ℃.

Of course, if the oxidative adsorption function of the second catalyst oxidizing adsorbent 420 decreases after a certain period of time, the second valve 320 is closed and the first valve 310 is opened to oxidize in the first catalyst oxidizing adsorbent 410. The adsorption action is caused to occur, and the second catalytic oxidation adsorbent 420 may be regenerated as described above.

As described above, the catalytic oxidation adsorption tower according to the present invention is composed of two adsorption oxidation spaces in parallel, so that the catalytic oxidation adsorbent is continuously used to purify the contaminated gas even during the regeneration of one catalytic oxidation adsorbent. You can do it. Therefore, the present invention can utilize the operation of the production equipment 100%.

In addition, the present invention can be used to regenerate the catalytic oxidation adsorbent several times through the regeneration operation to minimize the secondary waste generation problems, it is possible to reduce the operating cost.

For reference, the effects of the present invention in more detail through practical experiments and comparative examples are as follows.

Case 1 (Laboratory)

(1) Performance of the comparative object: existing granular activated carbon and catalytic oxidation adsorbent

(2) Comparative test method: Charge the same amount of activated carbon and catalytic oxidation adsorbent in the experimental adsorption tower

(3) Concentration and capacity of standard gas (pollutant) (see table 5 below)

Pollutant Type Initial concentration (ppm) Passing speed Remarks Benzene 200 ppm 1 L / min -Inspection method: detector tube (GASTEC)-gas after passing through the detector tube Toluene 300 ppm Aceton 450 ppm NH3 (ammonia) 500 ppm CH3SH (mercaptan) 60 ppm

(4) Date of analysis: November 22, 2002 (10: 00-17: 30)

(5) Experimental analysis result (see Table 6 below)

division Existing activated carbon Catalytic oxidation adsorbent Remarks Concentration after treatment Processing efficiency Concentration after treatment Processing efficiency benzene 140 ppm 30% 0 100% -30 seconds after gas passage-Activated carbon treatment efficiency: 10 ~ 36%-Catalytic oxidation adsorbent Treatment efficiency: 100%-After 5 minutes of measurement, the performance of activated carbon deteriorated rapidly, None. toluene 210 ppm 30% 0 100% Acetone 290 ppm 36% 0 100% ammonia 450 ppm 10% 0 100% Mercaptan 50 ppm 17% 0 100%

Application Case 2 (Site)

(1) Company name: S industry in Ulsan petrochemical complex

(2) Name of analysis gas (VOC's): Toluene & Aceton

(3) Application method: using existing activated carbon adsorption tower

-Filled with catalytic oxidation adsorbent (cardaros) as a substitute for activated carbon.

-Flow rate, flow rate (passing speed) and filter filling amount same as before

(4) Analysis method: direct measurement on site with Gastec

(5) Date of Analysis: June 5, 2003 PM 2: 00 ~ 7: 00

(6) Analysis results (see Table 7 below)

division Measuring time Before passing through adsorption tower After passing through adsorption tower efficiency(%) toluene 2 hours after replacement 4 hours after 700 ppm300 ppm60 ppm 0.6 ppm00 99.9100100 Acetone 2 hours after replacement 4 hours after 190 ppm250 ppm420 ppm 000 100100100

Case Study 3

(1) Comparison target: performance comparison of catalytic oxidation adsorbent and synthetic zeolite

(2) Comparative test method: After filling the same amount of catalytic oxidation adsorbent and synthetic zeolite in the experimental adsorption tower (P.P), select standard gas and contact it at a constant speed.

(3) Date of analysis: May 22, 2003

(4) Concentration of standard gas (pollutant) (see table 8 below)

Pollutant Type Initial concentration (ppm) Passing speed Remarks Benzene 53.2 ppm 1 L / min Inspection method: Quantitative analysis of gas after passing GC-MS Toluene 37.0 ppm Aceton 16.2ppm H2S (hydrogen sulfide) 10.0 ppm CH3SH (mercaptan) 10.0 ppm Dimethly sulfide (DMS) 10.0 ppm Dimethly disulfide (DMDS) 10.0 ppm

(5) Experimental analysis result (see Table 9 below)

division Synthetic zeolite Catalytic oxidation adsorbent Remarks Concentration after treatment Processing efficiency (%) Concentration after treatment (ppm) Processing efficiency (%) Benzene 10.6 79.9 0.0003 99.999 -30 seconds after the passage of gas-Synthetic zeolite treatment efficiency: 70 ~ 84%-Catalyst oxidation adsorbent Um.-filling amount: 330ml * 3-pass rate: 1 L / min Toluene 6.09 83.5 0 100 Aceton 4.89 69.8 0.0001 99.999 H2S - - 0.048 99.520 CH3SH - - 0 100 DMS - - 0 100 DMDS - - 0 100

As can be seen in the application examples described above, it can be seen that the application of the present invention significantly improves the removal of odors and volatile organic compounds.

As described above, since the catalytic oxidation adsorption tower according to the present invention has a parallel adsorption structure, the operation of the production facility can be utilized 100%, and the secondary wastes are generated because the catalyst oxidation adsorbent with reduced function is used several times. Costs can be minimized and operating costs can be reduced.

As described above, the present invention has been illustrated and described in connection with specific embodiments, but it is understood that various modifications and changes can be made without departing from the spirit and scope of the invention as indicated by the claims. Anyone who owns it can easily find out. For example, adsorption towers having a single structure, rather than parallel to the adsorption structure, should also be considered within the scope of the claims of the present invention if the internal configuration is the same or similar.

Claims (5)

The lower part is formed with an inlet through which contaminated gas is introduced, and an exhaust port through which gas is discharged is formed in the upper part, and the space between the inlet and the exhaust port is divided into a first space part and a second space part by a partition wall. An upper part of the first and second space parts is sealed by an upper partition, and a lower part of the adsorption tower structure is closed by a lower partition; First and second catalyst oxidizing adsorbents, each of which is installed at least one or more in the first and second space portions to oxidize and adsorb contaminants; Chemical injection means for spraying the regeneration solution only on the catalytic oxidation adsorbent which requires regeneration in the first and second catalyst oxidation adsorbents; Heater means for heating and drying only the catalytic oxidation adsorbent in which the regeneration solution is injected; And It is installed in the upper partition and the lower partition, and divided into a first valve at a position corresponding to the first space portion, and a second valve at a position corresponding to the second space portion, separate the first valve and the second valve Catalytic oxidation adsorption tower comprising a valve means for selectively on / off via the control unit. The method of claim 1, The catalytic oxidation adsorbent is a catalytic oxidation adsorption tower, characterized in that the inorganic oxidizing agent is ionically injected into the synthetic zeolite carrier is made by reversibly bonding. The method according to claim 1 or 2, The drug injection means Chemical tank with regeneration solution; A transfer pipe connected to the chemical tank to transfer regeneration solution; A plurality of distribution pipes connected to an end of the transport pipe to distribute the regeneration solution; A first chemical injection nozzle installed in the distribution pipe to spray the regeneration solution from the upper portion of the first catalytic oxidizing adsorbent, A second chemical spray nozzle installed in the distribution pipe to spray the regeneration solution from the upper portion of the second catalyst oxidizing adsorbent; A pump installed at a part of the conveying pipe and forcibly transferring the regeneration liquid of the chemical tank to the chemical spray nozzle; A catalytic oxidation adsorption tower comprising a chemical injection control unit for controlling the on / off of the first and second chemical injection nozzles, operation of the pump and injection time. The method according to claim 1 or 2, The heater means A first heater disposed under each of the first catalyst oxidizing adsorbents, A second heater disposed under each of the second catalyst oxidizing adsorbents, And a heater control unit for selectively operating the first and second heaters and controlling the temperature and the heating time. An adsorption tower structure in which a lower portion is formed with an inlet through which contaminated gas is introduced, and an exhaust port through which upper gas is discharged is formed; A catalytic oxidation adsorbent installed at least one inside the adsorption tower structure to oxidatively adsorb contaminants; A chemical spray nozzle installed on top of each of the catalytic oxidation adsorbents and spraying a regeneration solution when the function of the catalytic oxidation adsorbent is reduced; And A catalytic oxidation adsorption tower, characterized in that configured to include a heater that is installed to operate selectively under the respective catalytic oxidation adsorbent to dry the catalytic oxidation adsorbent.