Gaseous substance recirculation-type concentrator / oxidizer

Abstract

The present invention relates to a device for highly concentrating volatile organic compounds and an exhaust gas treatment device for treating same. The present invention provides a concentrator / oxidizer comprising: an adsorption concentrator for adsorbing and concentrating gaseous substances in exhaust gas discharged from an emission source; and an oxidizer for oxidizing the gaseous substances concentrated by the adsorption concentrator. The adsorption concentrator includes: an adsorption member, including an adsorption region, a desorption region, and a cooling region, for adsorbing, concentrating, and desorbing the gaseous substances in the exhaust gas discharged from the emission source; a plurality of streams including an exhaust gas stream for making the exhaust gas flow from the emission source into the adsorption region, a desorption gas stream for making desorption gas flow into and out of the desorption region, a cooling gas stream for making cooling gas flow into and out of the cooling region, and a recirculation stream that branches from the desorption gas stream discharged from the desorption region; and a heating means for heating the desorption gas stream that flows into the desorption region. The device includes the oxidizer, which is connected downstream of the cooling region, for oxidizing the gas branched from the cooling gas stream.

Description

Concentration oxidation device with gaseous material recirculation method

[0001] The present invention relates to a device for oxidizing waste gas containing gaseous substances such as odor, carbon dioxide, and volatile organic compounds, and more specifically, to a device for concentrating and oxidizing gaseous substances that remove low-concentration gaseous substances emitted from air purifiers, printing processes, painting processes, semiconductor processes, carbon dioxide emission facilities, and odor facilities by concentrating and then oxidizing them.

[0002] As legal regulations on the atmospheric environment strengthen, oxidation using heat or catalysts is increasingly being used as the safest method for gaseous substances containing both odors and volatile organic compounds. However, oxidation requires significant energy. Waste gases containing low concentrations of constituents have a low combustible content, so using high-temperature oxidation systems that utilize temperatures above 800°C or catalytic oxidation systems at temperatures above 300°C requires additional energy, increasing treatment costs.

[0003] Due to these problems, the regenerative thermal combustion method, which recovers heat by 95% or more using thermal storage materials and treats low-concentration volatile organic compounds, has been widely used recently. The regenerative thermal combustion method is an oxidation method that oxidizes volatile organic compounds at a high temperature by maintaining an oxidation temperature of 800℃ or higher. Generally, if the temperature can rise by 40-80℃ per cubic meter of gas due to the calorific value of the oxidation of volatile organic compounds in the gaseous substance, operation is possible without additional fuel supply. However, if the temperature rise is below 40℃ per cubic meter of gas, additional fuel is required.

[0004] Meanwhile, in the regenerative catalytic combustion method using a catalyst, the combustion temperature can be lowered to 200-450℃, so it can be processed more economically. In this case, if the calorific value per cubic meter of gas does not reach 10-30℃ due to the oxidation of volatile organic compounds contained in the gaseous substance, a lot of additional energy is consumed. In the actual painting process, gaseous substances containing odors and volatile organic compounds are often environments where volatile organic compounds are emitted at low concentrations. Therefore, in order to combust and oxidize low-concentration odors and volatile organic compounds, additional fuel must be added, and this has the disadvantage of high energy consumption and excessive maintenance costs.

[0005] To solve these problems, an oxidation device is being used that adsorbs waste gas containing low concentrations of gaseous substances on an adsorbent, desorbs it into a small amount of gas, concentrates the gaseous substances in the waste gas, and then combusts them using a regenerative combustor.

[0006] Figure 1 is a schematic diagram illustrating a conventional oxidation device.

[0007] Referring to Fig. 1, the oxidation device is configured to include an adsorption concentrator (10) and a regenerative combustor (20). The adsorption concentrator (10) includes an adsorption member forming functional regions including an adsorption region (A), a desorption region (D), and a cooling region (C) to adsorb and concentrate / desorb gaseous substances (pollutants) in waste gas, and a driving unit for relatively rotating the adsorption member with respect to the gaseous substances. In addition, the adsorption concentrator (10) may be equipped with a heating means (12) to desorb the pollutants adsorbed on the adsorption member, and the incoming waste gas may be branched and used as the desorbed gas. The gas concentrated and desorbed in the adsorption concentrator (10) is introduced into the regenerative combustor (20), combusted, and discharged. At this time, a portion of the combustion gas may be used as a heat source for the heating means (12).

[0008] Conventional oxidation devices, such as these, require significant energy for combustion of low-concentration waste gas, as the concentration of the concentrated gas is determined by the concentration of pollutants in the waste gas and the flow rate ratio (concentration ratio) of the inlet and desorbed gases. Furthermore, conventional oxidation devices require a large amount of thermal storage material to regenerate combustion energy, resulting in a large facility size and high initial investment costs.

[0009] In order to solve the problems of the above-mentioned prior art, the present invention aims to provide a gaseous substance concentration and oxidation device that concentrates and oxidizes gaseous substances in exhaust gas discharged from an emission source in a recirculation manner to a high concentration.

[0010] In addition, the present invention aims to provide a gaseous substance concentration and oxidation device that increases the concentration and temperature of gaseous substances and reduces the energy required for oxidation and desorption of concentrated pollutants by recirculating the desorbed concentrated exhaust gas to the front end of the adsorption member of the exhaust gas flow, the cooling inlet of a cooling area that recovers heat from the adsorption member of the concentrator, the cooling outlet, and / or the desorption inlet entering the area that desorbs adsorbed pollutants.

[0011] In addition, the present invention aims to provide a gaseous substance concentration and oxidation device that simplifies the configuration of the equipment by recovering energy transferred to the adsorption member during the desorption process as heat back to cooling air and attaching an oxidizer to the rear end thereof.

[0012] In addition, the present invention aims to provide a concentration oxidation device that enables combustion by concentrating low-concentration gaseous substances without using a separate heat exchange means when the concentration and temperature of the gaseous substance in the gas flow of the cooling outlet provide energy required for desorption and the waste gas temperature is higher than the oxidation initiation temperature of the gaseous substance.

[0013] In addition, the present invention aims to provide a concentrated oxidation device capable of adding a heat exchange means when the temperature of the waste gas entering the oxidizer does not reach the oxidation initiation temperature of the gaseous substance despite the oxidation heat of the concentrated gaseous substance.

[0014] In order to achieve the above technical task, the present invention provides an adsorption concentrator for adsorbing and concentrating a gaseous substance in an exhaust gas discharged from an emission source, and a concentration and oxidation device for oxidizing the gaseous substance concentrated by the adsorption concentrator, wherein the adsorption concentrator comprises: an adsorption member including an adsorption region, a desorption region, and a cooling region for adsorbing and concentrating and desorbing a gaseous substance in an exhaust gas discharged from an emission source; And a conduit providing a plurality of flows including an exhaust gas flow for introducing the exhaust gas from the emission source into the adsorption region, a desorption gas flow for introducing and discharging the desorption region and a cooling gas flow for introducing and discharging cooling gas into the cooling region, and a recirculation flow branched from the desorption gas flow discharged from the desorption region and joining at least one of the exhaust gas flow, the cooling gas flow, and the desorption gas flow, wherein the concentrated oxidation device includes a heating means for heating the desorption gas flow flowing into the desorption region, and an oxidizer for oxidizing the cooling gas flow or the gas branched from the cooling gas flow, and wherein the oxidizer discharge gas flow oxidized and discharged in the oxidizer flows into the desorption gas flow flowing into the desorption region or joins the desorption gas flow flowing into the desorption region.

[0015] In the present invention, the cooling region of the adsorption member may include a first cooling region and a second cooling region, a gas flow passing through the first cooling region may have a higher temperature than a gas flow passing through the second cooling region, and the first cooling gas flow passing through the first cooling region may be introduced into the oxidizer. In this case, the first cooling gas flow may be introduced into the oxidizer via the heating means.

[0016] The present invention includes a first oxidizer inlet gas stream branched from a first point of the cooling gas stream and provided to the oxidizer; and a first oxidizer exhaust gas stream discharged from the oxidizer and joining a second point of the cooling gas stream, wherein the first point may be a downstream point in the path of the gas stream than the second point.

[0017] Additionally, the present invention includes a first oxidizer inlet gas stream branched from a first point of the cooling gas stream and provided to the oxidizer; and a first oxidizer exhaust gas stream discharged from the oxidizer and joining a second point of the cooling gas stream, wherein the first point may be an upstream point on the path of the gas stream than the second point.

[0018] In the present invention, the oxidizer may be any one selected from the group consisting of a catalytic oxidizer, a catalytic oxidizer with an indirect heat exchanger, a regenerative oxidizer, and a regenerative catalytic oxidizer.

[0019] In the present invention, the first oxidizer inlet gas flow can be branched off at the rear end of the heating means.

[0020] In the present invention, the first oxidizer inlet gas flow can be branched when the concentration of the desorption gas flow is greater than a preset concentration.

[0021] The present invention may include a second oxidizer inlet gas stream branched from the desorption gas stream flowing into the desorption region and supplied to the oxidizer.

[0022] In this case, the purge gas passing through the above purge area can join the cooling gas flow flowing out from the cooling area.

[0023] In the present invention, the recirculating flow can join the cooling gas flow flowing into the cooling region.

[0024] In the present invention, the recirculation flow can join the exhaust gas flow flowing into the adsorption region.

[0025] In the present invention, the recirculating flow may be provided with a cooling means or a condensation recovery means.

[0026] In the present invention, the desorption gas flow may be provided with a cooling means.

[0027] In the present invention, a portion of the cooling gas flow may join the inlet gas flow.

[0028] According to the present invention, it is possible to provide a gaseous substance concentration and oxidation device that concentrates and oxidizes pollutant components in a low-concentration exhaust gas to a high concentration in a recirculation manner.

[0029] According to the present invention, a gaseous substance concentration and oxidation device can be provided that allows combustion of gaseous substances by providing a heat exchange function to an adsorption concentrator, oxidizing in an oxidizer, or using a heat exchange means such as a separate heat storage layer and heat exchanger without using a separate heat exchange means or using a minimum capacity by recirculating the energy recovered and the concentrated desorbed gas in a cooling area, thereby reducing the installation cost of combustion equipment.

[0030] According to the present invention, it is possible to provide a gaseous substance concentration and oxidation device capable of reducing the energy required for desorption of concentrated desorbed gas by providing a heat exchange function to an adsorption concentrator.

[0031] Figure 1 is a schematic diagram illustrating a conventional concentrated oxidation device.

[0032] FIG. 2a is a schematic diagram of a concentrated oxidation device for highly concentrating and processing a gaseous substance according to one embodiment of the present invention.

[0033] FIG. 2b is a schematic diagram of a concentrated oxidation device for highly concentrating and processing a gaseous substance according to another embodiment of the present invention.

[0034] FIG. 3 is a conceptual drawing illustrating that a cross-section of an adsorption member of a concentrator of the present invention is divided into multiple functional areas.

[0035] Figure 4 is a schematic drawing showing that the cross-section of the adsorption member of the concentrator of the present invention is divided into a plurality of functional areas and is divided into a primary cooling area and a secondary cooling area.

[0036] Figures 5 to 10 are schematic drawings showing embodiments according to other aspects of the present invention.

[0037] Figure 11 is a drawing showing one embodiment of an oxidizer used in the present invention.

[0038] Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the attached drawings. In describing the present invention, detailed descriptions of related known structures or functions will be omitted if they are deemed to obscure the gist of the present invention.

[0039] In the following specification of the present invention, gaseous substances include not only volatile organic compound components such as organic solvents such as toluene and NMP (N-Methyl-2-pyrrolidone), but also pollutants such as odor components, CO2, NO x It is used as a term to refer to all harmful substances such as water vapor. In addition, the term "gaseous substance" in the specification of the present invention may include water vapor.

[0040] Therefore, in the specification of the present invention, the gaseous substance may have different components depending on the type of gaseous substance, for example, it may refer to only an odor component, may refer to a gaseous substance component, or may refer to both an odor component and other harmful components.

[0041] FIG. 2a is a side view schematically illustrating a concentrated oxidation device according to one embodiment of the present invention.

[0042] Referring to FIG. 2a, the concentration oxidation device (100) includes an adsorption concentrator (110), a heating means (130), and an oxidizer (150).

[0043] Pollutants or hazardous components, i.e. gaseous substances, contained in exhaust gas flowing in from an emission source pass through an adsorption concentrator (110) and are adsorbed on the adsorbent material of the adsorption member of the adsorption concentrator (110) and then desorbed in a concentrated state. To this end, the adsorption concentrator (110) performs a series of processes of adsorbing pollutants on the adsorption member, concentrating and desorbing the adsorbed pollutants, and cooling the desorbed adsorption member.

[0044] The adsorption concentrator (110) of Fig. 2a can use an adsorption member as a means for adsorption concentrating a gaseous substance.

[0045] Figure 3 is a schematic drawing showing a cross-section of a cylindrical adsorption member constituting an adsorption concentrator.

[0046] Figure 3 is a schematic drawing showing a cross-section of an adsorption member (30) of the present invention, conceptually showing that the adsorption member (30) is divided into an adsorption region (A), a cooling region (C), and a desorption region (D).

[0047] In the present invention, the adsorption member (30) may be formed of an appropriate material having heat storage properties and gas adsorption properties. The adsorption member may generally be used by coating an adsorbent having excellent adsorption properties on a base material made of ceramic fiber, glass fiber, or aluminum or stainless steel metal plate folded. Of course, the present invention is not limited thereto, and the adsorption member (30) may be formed of one material selected from the group consisting of zeolite such as 3A, 4A, USY, or ZSM-5, MOF (metal organic framework), activated carbon, activated carbon fiber, CNT (carbon nanotube), graphene, alumina, silica, and polymer resin, or a composite material of the selected materials.

[0048] Additionally, materials such as SiC, alumina, silica, cordierite, and zirconia can be added to the above material to enhance heat storage properties.

[0049] In addition, the above adsorption member may be a rechargeable one using a spherical adsorbent, an amorphous adsorbent, a cylindrical adsorbent, and a honeycomb-shaped adsorbent, or a honeycomb-shaped adsorption member formed into a laminated adsorbent using a folded, extruded, or sheet-shaped adsorbent to improve breathability and contact area.

[0050] The above adsorption member may be composed of a multi-stage adsorption member. For example, the adsorption member may include a front end member facing the exhaust gas flow and a rear end member adjacent thereto, and the front end member and the rear end member may be composed of different materials. For example, the front end member may include one selected from the group consisting of silica, zeolite 3A, and 4A, diatomaceous earth, and MOF, which are hydrophilic adsorbents that adsorb moisture well, and the rear end member may include, as a main component, a zeolite (USY, ZSM5, beta, etc.) that has a low relative adsorption capacity for moisture but adsorbs volatile organic compounds well, and a hydrophobic zeolite among these zeolites having a Si / Al molar ratio of 15 or more.

[0051] As illustrated in FIG. 2a, in the present invention, a rotor-type adsorption concentrator capable of controlling the rotation speed according to the concentration of the gaseous substance introduced may be used as the adsorption concentrator (110). In this embodiment, the rotor of the adsorption concentrator (110) may rotate at a rotation speed of 2 to 20 rph. In the present invention, the rotation speed of the rotor is exemplary and may be set differently according to the process conditions or process conditions. In addition, the rotor may be applied in various forms as long as the adsorption concentrator can repeatedly perform the adsorption, cooling, and desorption processes by the rotation of the rotor, and it does not matter whether the rotation of the rotor is continuous or intermittent.

[0052] As described above, the gaseous substances contained in the exhaust gas of the emission source are introduced into the adsorption concentrator (110) and adsorbed in the adsorption area (A) of the adsorption member. As the rotor rotates, the adsorption member (10) that has adsorbed the gaseous substances enters the desorption area (D) and is desorbed by the desorption air. At this time, a gas having a lower flow rate than the exhaust gas introduced into the adsorption area (A) is used as the desorption gas. Preferably, the desorption gas flow rate and the adsorption gas flow rate are 1 / 3 to 1 / 30. Accordingly, the desorption gas can contain a high-concentration gaseous substance 3 to 30 times that of the adsorbed gas. The flow rate of the exhaust gas introduced into the adsorption area (A) and the flow rate of the desorption gas can be adjusted in ratio by adjusting the desorption gas transport means according to the concentration. However, if the amount of desorption gas is reduced too much, the desorption energy required for the desorption of the gaseous substances cannot be delivered, and thus desorption will not occur. Therefore, it must be appropriately adjusted.

[0053]

[0054] In the present invention, the concentrated oxidation device (100) has a plurality of gas streams and flow paths for implementing them. As illustrated, for example, appropriate flow paths are provided to provide an exhaust gas stream (①) from a pollutant source (or emission source) penetrating an internal adsorption member, a desorption gas stream (③, ③') that desorbs adsorbed gaseous substances, and a cooling gas stream (②, ②', ②") for cooling an area of ​​the adsorption member heated after desorption. In addition, appropriate flow paths are provided so that a portion of the desorption gas stream (③') branches off as a recirculation stream (④) and joins the cooling gas stream (②'), and another portion is connected to the exhaust gas stream (⑤) and discharged.

[0055] In the present invention, various sources may be added to the cooling gas flow (②). For example, outside air, exhaust gas from a pollutant, or purified gas may be used. Here, the outside air may include clean atmospheric air, air with an adjusted oxygen concentration, or, in the case where the combustible material is a gaseous substance, an inert gas such as non-reactive nitrogen, carbon dioxide, and helium. This cooling gas flow (②) is mixed with the circulating recirculation flow (④) of the desorption gas flow (③') to form a cooling gas flow (②").

[0056] In the illustrated embodiment, the exhaust gas from the emission source (pollution source) is used as the cooling gas flow (②). In this case, as illustrated, some of the exhaust gas from the emission source branches off from the exhaust gas flow (①) and joins the cooling gas flow. The ratio of the flow of the branched cooling gas to the exhaust gas flow (①) determines the content of the pollutant component in the desorbed gas, and therefore, this ratio can regulate the concentration multiple. For example, the ratio of the exhaust gas used as the cooling gas is determined by the amount of the desorbed gas and the recirculation rate. The flow rate ratio of (exhaust gas flow rate) / (desorbed gas flow rate) is not particularly limited, but must be an amount that can provide the energy required for desorption of the adsorbed gaseous substance. Generally, 3 to 30 times is mainly used in the field, and when the recirculation rate is 50% (i.e., when 50% of the desorbed gas is recirculated as cooling gas), the flow rate ratio of (exhaust gas flow rate) / (branched cooling gas flow rate) increases to 6 to 60.

[0057] In addition, in the present invention, the concentrated oxidation device (100) may be provided with appropriate gaseous substance transfer means, sensors, gas inlets, gas outlets, and a housing. In addition, appropriate valves for branching the recirculation flow and the exhaust flow, ducts for forming a flow path, and a blower may be provided. In addition, in the present invention, a plurality of flow paths penetrating the adsorption member are separated and / or partitioned by appropriate sealing means so that the gas flows therebetween do not interfere with each other. For example, by arranging a silicone resin, a heat-resistant polymer, or a metal or ceramic material between the housing and the adsorption member, the gas flow flowing through each flow path can be separated and partitioned.

[0058] Meanwhile, the cooling gas flow (②') passes through the cooling area (C) and is further heated by the heating means (130) and then flows into the desorption area (D). It goes without saying that the heating means (130) of the present invention may be implemented as a part of the concentrating device (100) or may be implemented as a separate, distinct component.

[0059] In the present invention, the plurality of regions may be defined as areas substantially perpendicular to the gas flow flowing through the flows (①, ②', ③) described with reference to FIG. 2a. For example, the area of ​​the region may be defined by a cross-sectional area perpendicular to the axial direction of the concentrator (110).

[0060] The above multiple regions may include functional regions such as, for example, an adsorption region (32), a desorption region (34), and a cooling region (36).

[0061] In the above-described adsorption member of the present invention, the areas occupied by the adsorption region (32), the desorption region (34), and the cooling region (36) can be appropriately divided. In general, the area of ​​the adsorption region (32) can preferably occupy 40% to 90% of the total area of ​​the adsorption member (30). Therefore, the adsorption region (32) can have a larger area than the desorption region (34) or the cooling region (36). In addition, the desorption region (34) and the cooling region (36) can be designed to have the same area, or the desorption region (34) can be designed to be smaller than the cooling region (36).

[0062] Preferably, in the present invention, the relationship of adsorption area > cooling area ≥ desorption area may be maintained. Specifically, in the present invention, the cooling area / desorption area ratio may be 1.05 or more, 1.1 or more, or 1.2 or more. In addition, the upper limit of the area ratio may be limited to 1.5, 2.0, or 3.0. An excessive area ratio exceeding this does not substantially affect the increase in energy recovery efficiency, and is therefore disadvantageous from an economic perspective. However, the area area may vary depending on process conditions. For example, the area of ​​the cooling area may be smaller than the area of ​​the desorption area.

[0063] Meanwhile, as illustrated, the functional area of ​​the adsorption member (30) in the present invention may further include a purge area (28).

[0064] The purge zone (38) shown in Fig. 2a may be considered as an additional zone added to the cooling zone. When the recirculation rate increases or the temperature and concentration of the concentrated gas coming from the desorption zone increase, it is necessary to purge it, and for this purpose, a purge zone (28) may be added. At this time, the purge gas introduced into the purge zone (38) may be one type of gas selected from among external air, exhaust gas, and purified exhaust gas, or a mixture thereof. Here, the external air may include clean atmospheric air, air with controlled oxygen concentration, and, in the case where the combustible material is a gaseous substance, inert gases such as non-reactive nitrogen, carbon dioxide, and helium.

[0065] In the present invention, the adsorption member (30) functions as a plurality of regions, such as an adsorption region (32), a desorption region (34), a cooling region (36), and a purge region (38), when in operation, and these regions can be isolated or separated by a sealing means.

[0066] The concentrated oxidation device (100) of the present invention comprises a heating means (130) for heating the desorbed gas. In the present invention, the heating means (130) may be a heating device such as a heater, microwave, or plasma (or plasma burner), or a vibration means such as an ultrasonic vibrator. Of course, the present invention is not limited thereto, and various heating means may be used, but preferably, an electric heater, a burner, and high-temperature air are used as the heating device. When high-temperature air is used, a method of directly introducing it into the desorbed gas flow or transferring heat energy through an indirect heat exchanger may be used.

[0067] As previously described, a portion of the desorbed gas is branched off and rejoins the cooling gas flow. This branching mechanism may comprise a gas flow conveying means such as a blower, ducts, sensors, and valves.

[0068] In the present invention, the exhaust gas recirculation stream (④) passing through the recirculation duct contains gaseous substances that are concentrated and have a high concentration compared to the exhaust gas stream (①). In the present invention, the concentration concentration can be determined according to the concentration multiple and the recirculation rate. For example, in the present invention, when the ratio of the desorbed gas to the exhaust gas of the emission source is 15 times, the concentration concentration can be increased up to 300 times by changing the circulation rate from 5 to 95%, and when the actual treatment rate is considered to be 95%, it is 0.25 g / Nm. 3 The exhaust gas is 71.262 g / Nm 3 It can be concentrated to obtain a concentration of up to 285 times.

[0069] Therefore, the cooling gas stream (②') mixed with the concentrated exhaust gas recirculation stream in this way contains a high concentration of gaseous substances.

[0070] The cooling gas flow (②') is heated by the heating means (130) and flows into the desorption area (D) of the adsorption member (10) to desorb the adsorbed gas, thereby making the desorbed gas flow (③') passing through the adsorption member more concentrated. In this way, the concentration of pollutants in the exhaust gas recirculation flow (④), the cooling gas flow (②'), and the desorbed gas flow (③') increases due to repetition of adsorption, cooling, and desorption, and after several repetitions, reaches a certain concentration selected by the driver, i.e., an equilibrium concentration.

[0071] Combustible materials pose a risk of fire or explosion in the presence of oxygen. Therefore, they should be managed below their LEL. However, to ensure safety, it is recommended to maintain a level of 25% of the LEL. Since the LEL varies with ambient temperature, its influence on temperature should also be considered when determining the LEL. However, in cases where this risk is not present, it is permissible to set the LEL at a concentration suitable for condensation, recovery, and oxidation.

[0072] In general, when desorption is performed by applying heat, the temperature of the desorption gas must be higher than the adsorption temperature, and the temperature is preferably 100 to 300°C. The desorption gas temperature may vary depending on the gaseous substance to be adsorbed and the characteristics of the adsorption material.

[0073] Meanwhile, in order to use the desorbed gas as a recirculating stream in the present invention, some or all of the desorbed gas may be heat-exchanged. For example, when desorbing at a gas temperature of 220°C, the gas concentrated after desorption transfers heat to the member in the desorption area and is discharged at a temperature of approximately 40 to 100°C or lower. However, when this gas is recirculated, especially when recirculated to the adsorption inlet, the temperature of the gas may rise somewhat, so it is necessary to lower the temperature of the desorbed and recirculated gas. At this time, various means such as an air-cooled heat exchanger, a water-cooled heat exchanger, and a refrigerator can be used as a cooling means, but a water-cooled heat exchanger type is generally preferred. In addition, in the present invention, the heat exchanger may be installed in a branched flow path for recirculation, or, in the case of cooling condensation or recovery, it may be installed before the circulated gas and the discharged gas are diverged.

[0074] By the above mechanism, the low-concentration gaseous substance of the exhaust gas flow (①) of the initial emission source is introduced into the concentrator, and as the concentrator rotor rotates, the gaseous substance is repeatedly adsorbed → desorbed → cooled → adsorbed → desorbed → cooled in that order, so that the exhaust gas flow can be gradually concentrated into a high-concentration gaseous substance.

[0075] In the present invention, the concentration of the circulated exhaust gas is higher than the concentration of the inflow, and the temperature and concentration of the cooling gas are higher than in the case where it is not circulated due to the heat transferred during the desorption process. At this time, the exhaust gas with high concentration remains in the adsorption member and when it goes to the adsorption area, it may not be adsorbed in the adsorption area and may immediately escape. Although the effect caused by this is not large, a purge area that does not include the circulated exhaust gas can be provided to eliminate the effect and lower the temperature. The purge area (28) can be used by injecting outside air, exhaust gas from the emission source, or purified gas to perform the purge. Here, the outside air may include clean atmospheric air, air with adjusted oxygen concentration, or inert gases such as non-reactive nitrogen, carbon dioxide, and helium when the combustible material is a gaseous substance.

[0076] In this case, the gas flows passing through the cooling zone and purge zone can be separated or combined. The gases passing through the cooling zone and purge zone can be mixed, heated by a heating means, and then introduced into the desorption zone, so they do not necessarily need to be separated into separate compartments.

[0077] In one embodiment of the present invention, the exhaust gas from the exhaust source may be used as the purge gas in the purge region. Furthermore, in one embodiment of the present invention, the purge gas passing through the purge region may join a cooling gas flow. The purge gas joined with the cooling gas flow may form a desorption gas flow.

[0078] When using the purge region, gaseous substances can be concentrated by sequentially switching in the order of adsorption → desorption → cooling → purge → adsorption → desorption → cooling → purge.

[0079] In the present invention, the concentration ratio of the gaseous substance in the exhaust gas can be controlled by the percentage of the flow rate of the recirculation flow (④) to the flow rate of the desorption gas flow (③'), i.e., the recirculation rate. In the present invention, the recirculation rate can be controlled according to the concentration of the gaseous substance in at least one of the exhaust gas flow flowing into the adsorption member from the emission source, the recirculation gas flow flowing into the adsorption member (cooling region), and the gas flow passing through the adsorption member. In the present invention, the recirculation rate can be from 1 to 99.9%, but preferably from 5 to 95%. For example, the recirculation rate can be 5% or more, 10% or more, 15% or more, or 20% or more. In addition, the recirculation rate can be 95% or less, 90% or less, 85% or less, or 80% or less.

[0080] For example, the concentration of gaseous substances being introduced or recirculated can be designed to be maintained below the lower explosive limit (LEL) that explodes due to the introduction of oxygen. Preferably, the present invention is designed to control the recirculation flow (④) and the desorbed gas flow (③') at a constant ratio in consideration of safety, since the temperature of the exhaust gas containing combustible vapors that may explode is not constant, thereby maintaining the concentration at 1 / 4 to 1 / 5 of the lower explosive limit. For example, in the case of Table 1, the lower explosive limit of toluene is 52.2 g / Nm 3 and 1 / 4 of this is 13.05 g / Nm 3 If the concentration is 13.05 g / Nm 3 If you want to control it below, the concentration is 0.25 g / Nm 3 In this case, if the recycling rate is 80%, it is 14.263 g / Nm 3 Since concentration is possible up to 0.5 g / Nm, a smaller value is set and the concentration is 0.5 g / Nm. 3 If 60% is recycled, 14.275 g / Nm 3 Since concentration is possible up to this point, it is desirable to set a lower recirculation rate.

[0081] The device of the present invention may be equipped with a concentration sensor (125) for measuring the concentration of gaseous substances in order to control the recirculation rate. In Fig. 2a, the concentration sensor is installed upstream of the adsorption area of ​​the adsorption member (10) in the exhaust gas flow, but this is exemplary, and the concentration sensor may be installed on an appropriate flow path before the flow into the adsorption member (10) of the concentrator. Of course, the concentration sensor may be installed on the flow path of the desorption gas flow, or may be installed on all of the flow paths upstream of the adsorption member, the desorption gas flow path, and the cooling gas flow path. In addition, an additional concentration sensor (126) may be installed on the gas flow path passing through the adsorption member. This downstream concentration sensor (126) is for controlling the adsorption efficiency so that the concentration at the downstream of the adsorption member does not increase above a certain level.

[0082] In the present invention, the concentration oxidation device (100) includes an oxidizer (150). In the present invention, the oxidizer (150) is connected to the rear end of the cooling region (26) of the adsorption concentrator (110) in the gas flow path, and a cooling gas flow (②', ②") that has passed through the cooling region flows into the oxidizer (150). This is different from the conventional concentration oxidation device in which the oxidizer is connected to the rear end of the desorption region (24) in the gas flow path, and a concentrated exhaust gas flow (⑤) flows into the oxidizer.

[0083] In the present invention, the oxidizer (150) may be an oxidizer capable of oxidizing the concentration and temperature of the concentrated pollutants discharged from the cooling outlet without adding separate energy or with low energy. For example, the present invention may use a catalytic oxidizer capable of oxidizing pollutants at 50 to 400 degrees, and more preferably, a catalytic oxidizer capable of initiating an oxidation reaction of the concentrated pollutants at 120 to 300 degrees. However, the present invention does not exclude the use of an oxidation device equipped with a heat exchange means, such as a conventional regenerative oxidizer, a catalytic oxidizer with a heat exchanger attached, or a high-temperature oxidizer with a heat exchanger attached, in order to process a gas that is highly concentrated and concentrated at a temperature of 120 to 300 degrees discharged from the cooling outlet by recovering energy from the adsorption member. Here, the regenerative thermal oxidizer is an RTO (Regenerative Thermal Oxidizer), RCO (Regenerative Catalyst Oxidizer), etc., and refers to an oxidizer that divides the regenerative material into a process gas inlet area and a combustion gas exhaust area, and regenerates the energy accumulated in the regenerative material in the exhaust area as a heat source in the inlet area. When an oxidizer with a regenerative layer and a heat exchanger is used, the structure may be complicated and the installation cost and installation area may increase, but it can be applied in cases where a catalytic oxidizer, regenerative thermal oxidizer, or regenerative catalytic oxidizer cannot be used due to a low cooling outlet temperature.

[0084] In the present invention, the catalytic combustor may be equipped with an oxidation catalyst. The oxidation catalyst may be a porous body having a high specific surface area and containing a catalytic component. The catalytic component includes at least one component selected from the group consisting of Pt, Pd, Rh, Ru, Cu, Mn, Co, Mo, Ti, V, W, Ni, Ag, Au, Fe, Os, Ga, In, Tl, Pb, Ir, Zr, Ta, Hf, Tc, Re, Sn, Cr, Zn, Li, Na, K, Rb, Cs, Be, Mg, Ca, Sr, Ba, Y, La, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and Ce. When the oxidation means is a catalytic oxidizer, any oxidation catalyst, such as a noble metal group catalyst, a transition metal catalyst, and a perovskite catalyst, may be used. The above catalyst component can be prepared by supporting or ion-exchanging the above porous body, or by co-precipitating the catalyst component with an adsorbent. In addition, the shape of the carrier can be spherical or cylindrical, and alternatively, it includes a carrier supported, ion-exchanged, coated, or formed into an extruded honeycomb or a polarized molded honeycomb, or formed into the catalyst particle itself.

[0085] In addition, when using a catalytic oxidizer, the amount of catalyst is determined by the gas hourly space velocity (GHSV) per unit volume of catalyst, which is used in the range of 1,000 to 100,000 hr-1 depending on the catalyst component, but is not limited. However, the range for general precious metals and transition metals is preferably 5,000 to 50,000 hr-1.

[0086] The operating mechanism of the concentrated oxidation device in the present invention is as follows.

[0087] In the present invention, the temperature of the gas passing through the adsorption concentrator during operation of the adsorption concentrator can change as follows.

[0088] After desorption by the desorption gas flowing into the desorption area of ​​the adsorption member from the heating means, the adsorption member in the desorption area becomes a cooling area and is cooled by the cooling gas flow.

[0089] At this time, the temperature of the desorption gas flow (③) flowing into the adsorption concentrator (110) is maintained at a predetermined set temperature. For example, when the set temperature of the desorption gas flow (③) is 220°C, the desorption gas flow (③') at the outlet of the adsorption concentrator may vary depending on the accumulation capability of the adsorption member and the rotation speed of the adsorption member, but is approximately 50 to 100°C.

[0090] At this time, in the present invention, all or part of the desorption gas flow (③') branches off to form a recirculation flow (④), which joins with the cooling gas flow (②) and flows into the cooling area of ​​the adsorption member. The cooling gas flow passes through the adsorption member and cools the cooling area, and the temperature of the cooling gas flow (②") that has passed through the cooling area becomes approximately 150 to 200°C. Of course, the temperature of the cooling gas flow (②") mentioned is an example, and can be controlled within 60 to 90°C (based on Celsius) of the temperature of the desorption gas flow (③) depending on other process conditions such as the recirculation rate. Therefore, assuming that the temperature of the cooling gas flow (②") is 170°C, the heating means can maintain the preset temperature as the desorption gas flow (③), that is, 220°C, by increasing the temperature by only approximately 50°C.

[0091] Meanwhile, in the present invention, when the concentration of the desorption gas stream (③) is higher than a preset concentration, a portion of the desorption gas stream (③) flowing into the desorption region is branched and supplied to the oxidizer (150). In the present invention, the concentration of the oxidizer inlet gas stream (⑦) can be determined based on the calorific value of the pollutant component in the gas stream. When the pollutant component is toluene, combustion of about 440 ppm of toluene can increase the gas temperature after oxidation by about 50 ℃. Therefore, the exhaust gas of the oxidizer has a temperature of about 270 ℃, and by joining the first oxidizer exhaust gas stream (⑧) with the cooling gas stream (②") which is relatively low temperature (about 170 ℃), the temperature of 220 ℃, which is the set temperature of the desorption gas stream (③), can be achieved. However, it is assumed that the flow rates of the first oxidizer exhaust gas stream (⑧) and the cooling gas stream (②") are the same. Accordingly, the energy required for the heating means (130) can be reduced, or preferably, the operation of the adsorption concentrator can be achieved without a separate energy supply to the heating means. In this case, the desorption gas flow (③) can bypass the heating means (130).

[0092] As described above, according to one aspect of the present invention, when the concentration of a pollutant component in the desorbed gas stream (③') flowing out from the adsorption concentrator is lower than a preset concentration (for example, a preset concentration of 440 ppm or more based on toluene), part or all of it may be recycled to the adsorption concentrator. In addition, according to one aspect of the present invention, the concentration of the pollutant component in the gas increases by the recirculation, and when the concentration of the pollutant component reaches the preset concentration, at least a part of the desorbed gas stream (③') is branched. In addition, according to one aspect of the present invention, the gas branched from the desorbed gas stream (③') is introduced into the oxidizer (150) by the recirculation flow and is combusted in the oxidizer (150). The combustion gas, the temperature of which has increased due to combustion within the oxidizer (150), may join the cooling gas flow (②") as the first oxidizer exhaust gas flow (⑧) and be provided as a desorption gas flow (③). At this time, the joining point (A) of the first exhaust gas flow (⑧) may be upstream of the branch point (B) of the desorption gas flow flowing into the oxidizer.

[0093] The device of the present invention may be provided with a second oxidizer inlet gas stream (⑥) for supplying the concentrator exhaust gas stream (⑤) to the oxidizer. In the present invention, the flow rate of the second oxidizer inlet gas stream (⑥) may be set in consideration of the recirculation rate. In addition, when the concentration of the pollutant component in the desorption gas stream (③') is higher than a preset concentration, the desorption gas stream (③') is provided as the concentrator exhaust gas stream (⑤), and all or part of it may be introduced as the second oxidizer inlet gas stream (⑥) and supplied to the oxidizer. At this time, when the oxidizer (150) is configured as a heating device + catalyst 1 + catalyst 2 in consideration of the balance of temperature and concentration when using a catalytic oxidizer, the second oxidizer inlet gas stream (⑥) may be supplied between the catalyst 1 and catalyst 2 of the oxidizer. That is, there is no reason to limit it to any one of the front, middle, and rear ends where it is introduced into the oxidizer.

[0094] Meanwhile, in order to balance the mass balance inside the device in the present invention, a portion of the gas combusted in the oxidizer (150) may be discharged outside the device as a second oxidizer exhaust gas flow (⑨).

[0095] Meanwhile, although the case where the recirculation flow branched from the ideal desorption gas joins as a cooling gas flow (②') has been described, the present invention is not limited thereto, and it goes without saying that a different design of the recirculation path can be applied to increase the concentration of the desorption gas. For example, Fig. 2a illustrates another recirculation gas flow (⑩) joining the exhaust gas flow (①). In the present invention, the recirculation gas flow (⑩) can be provided simultaneously with the aforementioned recirculation flow (④) or can be provided independently of the recirculation flow.

[0096] As described above, the present invention can suppress the discharge of gas to the outside of the device by setting the recirculation rate of the recirculation flow to the maximum when the concentration of pollutants in the exhaust gas of the emission source is low, and on the other hand, when the concentration of pollutants increases to a certain extent, the gas that has passed through the oxidizer can be discharged to the outside while adjusting the recirculation rate to balance the material balance.

[0097] In the present invention, the oxidizer (150) and the heating means (130) may be provided in the form of an assembly coupled to the concentration oxidizer (110). Fig. 12 is a diagram schematically illustrating such an example.

[0098] Referring to FIG. 12, an oxidation catalyst layer (150) may be provided on the cooling zone outlet side and the desorption zone inlet side of a concentration oxidizer (110), a catalyst chamber (152) in which the oxidation catalyst layer (150) is installed may be coupled to a concentration member (10), and a desorption chamber (132) equipped with a heating means (130) may be coupled to the catalyst chamber (154).

[0099] Fig. 4 is a schematic diagram illustrating another example of an adsorption member used in the present invention. As illustrated in Fig. 4, the adsorption member may include a first cooling region and a second cooling region.

[0100] A concentrated oxidation device including the adsorption member of Fig. 4 may have the following configuration.

[0101] A concentration-oxidation device comprising an adsorption concentrator for adsorbing and concentrating gaseous substances in an exhaust gas discharged from an emission source, and an oxidizer for oxidizing the gaseous substances concentrated by the adsorption concentrator. At this time, the adsorption concentrator includes an adsorption member including an adsorption region, a desorption region, a first cooling region, and a second cooling region for adsorbing and concentrating and desorbing gaseous substances in an exhaust gas discharged from the emission source, and includes a plurality of flows including an exhaust gas flow for introducing the exhaust gas from the emission source into the adsorption region, a desorbed gas flow flowing into and out of the desorption region, and a first recirculation flow branching from the desorbed gas flow discharged from the desorption region and passing through the first cooling region, and a heating means for heating the desorbed gas flow flowing into the desorption region, and the device may include an oxidizer at any one position among (a) a rear end of the first cooling region, (b) a front end of the desorption region, or (c) a point branched from the flow between the cooling region and the desorption region, among the gas flows between the first cooling region and the desorption region. The oxidizer can be a catalytic oxidizer, a thermal accumulator, or a thermal accumulator catalytic oxidizer.

[0102] Figure 2b is a schematic diagram of a concentrated oxidation device for highly concentrating and processing gaseous substances according to another embodiment of the present invention. In Figure 2b, the same reference numerals as in Figure 2a denote the same elements, and redundant descriptions are omitted.

[0103] As illustrated in FIG. 2b, the concentration oxidation device may include an adsorption concentrator (110), a heating means (130), and an oxidizer (150), and may include blowers such as an adsorption blower (121) and a recirculation blower (122). In addition, the device may include various sensors and auxiliary devices for controlling and monitoring these components.

[0104] The present invention desorbs a gas flow adsorbed on an adsorption member (110) by a desorption gas flow (③) in a desorption zone (D) from an adsorption member (110), and the highly concentrated desorption gas flow (③) is recirculated to any point of the exhaust gas flow (①), the cooling gas flow (②, ②'), and the cooling zone (C1, C2) and the desorption zone (D) by a recirculation blower (122). Although FIG. 2b illustrates that three recirculation streams (①, ②, ②') coexist, in the present invention, the recirculation may be composed of one or more combinations of these recirculation streams.

[0105] The three recirculating flows illustrated in FIG. 2b first increase the concentration of pollutants in the gas flow flowing into the oxidizer (150), and the cooling zones (C1, C2) serve to increase the temperature of the gas flowing into the oxidizer (150). Therefore, the air flowing into the oxidizer (150) by the recirculating flow and the cooling gas flow has a higher temperature and a higher concentrated gas concentration than before. As illustrated, the adsorption member of FIG. 2b is composed of two cooling zones (C1) and a cooling zone (C2), and the oxidizer (150) is provided between the cooling outlet and the desorption inlet of the cooling zone (C1).

[0106] As illustrated, when the cooling zone is divided into C1 and C2, the gas flow (②') passing through C1 has a high concentration and temperature, and the gas flow passing through C2 has a relatively low concentration and temperature compared to the gas flow passing through C1. Therefore, by installing an oxidizer (150) in the gas flow (②') passing through C1, the gas flow flowing into the oxidizer (150) can be configured to be closer to the oxidation initiation temperature. If the gas flow flowing into the oxidizer (150) does not reach the oxidation initiation temperature of the oxidizer (150), energy can be supplied by the heating means (130). Gaseous pollutants that reach the oxidation initiation temperature in the oxidizer (150) are oxidized in the oxidizer (150) to generate oxidation heat, which can be used as an energy source for desorption. Therefore, if the concentration of the gas flow flowing into the oxidizer (150) is high, the oxidation heat increases and it becomes possible to perform a desorption operation without adding additional energy by the heating means (130).

[0107] Meanwhile, if the temperature of the gas flow (②') in the cooling area (C1) is too low, an additional heat exchange means may be installed in the gas flow (②') entering the heating means and the oxidizer. The heat exchange means may be a recuperative heat exchanger or a regenerative heat exchanger. If the heat of oxidation produced in the oxidizer (150) is too high in energy and the temperature of the oxidizer (150) increases or the desorption inlet temperature becomes too high, the heat may be discharged to the outside from the oxidizer (150) or reused. The point of discharge to the outside may be the oxidizer (150) or any point between the desorption gas flow (3) and the rear end of the oxidizer.

[0108] Although Fig. 2b illustrates that the outlets of the two cooling zones are connected by separate conduits, it should be understood that in the present invention, the outlets of the two cooling zones may be formed by a single conduit.

[0109] Hereinafter, various embodiments of a concentrated oxidation device according to the present invention will be described. While various embodiments of the present invention will be described below, it should be understood that, if necessary, sensors for measuring gas flow, dampers for controlling the flow direction and volume of gas, and blowers for transporting the gas flow, etc., may be added at appropriate locations. Furthermore, the direction of gas flow described in the following specifications and drawings may be appropriately modified.

[0110] In the present invention, a heating means and an oxidizer may be arranged in series on a gas flow path in which a cooling gas flow flowing out of a cooling region leads to a desorption gas flow flowing into a desorption region. At this time, the oxidizer may be located downstream or upstream of the heating means on the gas flow path, and furthermore, the oxidizer and the heating means may be arranged at various points between the cooling gas flow and the desorption gas flow, and gases branched from various points on the gas flow path may flow into the oxidizer and the heating means. A schematic configuration and gas flow of the device of the present invention having various arrangements as described above are illustrated in FIGS. 5 to 10.

[0111] In the drawings below, each device can be represented by a five-digit code such as XXXXX, and the meanings of the letters or numbers used in each code are as follows.

[0112] First digit code: D if there are two cooling lines (Cooling 1, Cooling 2) and both the inlet and outlet are separate, S if the cooling lines are separate at the inlet and mixed at the outlet / the purge line is also mixed

[0113] Second digit code: If process A is applied, where the recirculation flow enters the cooling line, then O is indicated. If process A is not applied, then O is indicated.

[0114] Third digit code: If process B is applied, where the recirculation flow enters the inlet line, it is marked as O if process B is not applied.

[0115] Fourth digit code: If process C is applied, where the recirculation flow enters the desorption inlet line, it is marked as O if process C is not applied.

[0116] Fifth digit code: This indicates the application location when applying the oxidizer. 1 is the desorption line, 2 is the cooling 1 line, and R is used when the circulation cycle is branched from the cooling outlet line.

[0117] In the drawings, dotted lines represent various options for connecting gas flows, and indicate that if one of these dotted lines is connected, the other dotted lines may not be connected. For example, in the case of SAOO1, Process A is applied where the circulation enters the cooling line, and at least one of the dotted lines that flows from the cooling outlet to the heating means (130) and the oxidizer (150) is sufficient. In addition, the solid line that does not enter the desorption inlet in the oxidizer but is discharged to the outside means that the oxidizer treats it harmlessly and discharges it to the outside.

[0118] Meanwhile, SOBO1 is a recirculation line that enters the adsorption after the desorption, and can be recirculated to either a location before or after the cooling air is branched off from the section entering the adsorption, and both can be installed. However, the arrow in the dotted line that discharges to the outside in the oxidizer (150) means that it does not have to be discharged to the outside.

[0119] Also, the explanation for DABC2 of Fig. 8g is as follows.

[0120] The exhaust gas stream from the emission source passes through the adsorption area (A) of the adsorption member and is purified. The second cooling gas stream, which branches off from the exhaust gas stream and flows into the secondary cooling area (C2), passes through the secondary cooling area (C2) of the adsorption member, and then passes through the primary cooling area to join the first cooling gas stream that has passed through the heating means (130) and the oxidizer (150). However, all or part of the second cooling gas stream may branch off and be mixed at any point with the exhaust gas stream that has passed through the adsorption area (A) or the primary cooling area (C1) and then be discharged to the outside. When discharged to the outside, the concentration of pollutants in the second cooling gas stream can be directly or indirectly checked and then discharged. When the concentration of the exhaust gas to be treated is high or highly hazardous, an external gas, rather than the exhaust gas of the emission source, can be used as the second cooling gas stream. At this time, the external gas may include clean atmospheric air, purified exhaust gas, or air with adjusted oxygen concentration, and in the case of combustible substances in the form of gas, inert gases such as non-reactive nitrogen, carbon dioxide, and helium.

[0121] In this example, the first cooling gas flow passing through the primary cooling zone (C1) is a high-concentration concentrated gas desorbed in the desorption zone (D) that is branched off and recirculated. When this first cooling gas flow passes through the primary cooling zone (C1), heat exchange occurs between the high-concentration concentrated gas desorbed in the desorption zone (D) and the heated adsorbent, resulting in a high-concentration, high-temperature concentrated gas. At this time, the adsorbent that has passed through the desorption zone (D) is heated to a high temperature, making it difficult to re-adsorb contaminants in the recirculated concentrated gas. Therefore, if the temperature of the adsorbent is sufficiently high during the cooling process, the contaminants in the concentrated gas can escape from the primary cooling zone (C1) with little adsorption. In this case, when the temperature required for oxidation in the oxidizer (150) is formed, the contaminants in the concentrated gas are introduced into the oxidizer (150) and oxidized without additional heating by the heating means (130). If the temperature required for oxidation in the oxidizer (150) is insufficient, additional heating can be applied. In this way, the first cooling gas flow heated by the heating means (130) or the oxidizer (150) joins with the second cooling gas flow to form a desorption gas flow. The pollutants adsorbed in the adsorption area (D) of the adsorption member are desorbed and concentrated by the high-temperature desorption gas flow. At this time, the concentrated desorption gas flow is shown to be recirculated between the first cooling area (C1), the exhaust gas flow from the emission source, and the desorption gas flow before the first cooling gas flow that passed through the first cooling area (C1) enters the desorption area (D). The recirculation flow that branches off from the desorption gas flow and circulates into the exhaust gas flow can join before or after the second cooling gas flow branches off. The recirculation flow that branches off from the desorption gas flow and recirculates to the front end of the desorption area (D) can be recirculated after the heating means (130) and after the oxidizer (150), but is not particularly limited thereto.

[0122] Meanwhile, in the case where the desorption gas stream is recycled as in the present invention, the cooling gas stream branched off from the exhaust gas stream flows into the cooling zone (C), cools the adsorption member, and recovers heat before exiting. At this time, the cooling gas stream from which the heat has been recovered desorbs the contaminants adsorbed on the adsorption member into which the desorption gas stream from the oxidizer (150) flows into the desorption zone (D). The concentration of the contaminants in the desorption gas stream increases, and this desorption gas stream is recycled back to the front end of the heating means, where it is mixed with the cooling gas stream that has passed through the cooling zone described above and flows into the desorption means. The introduced gas stream passes through the heating means and the oxidizer, oxidizing the contaminants and using the energy obtained thereby as desorption energy. In this process, the flow rates of the cooling gas stream and the desorption gas stream differ by the amount of recirculation, and thus, cooling may be reduced in the cooling zone due to the flow rate difference. Therefore, the problem of cooling degradation can be solved by increasing the cooling gas flow rate passing through the cooling region to be similar to the desorption gas flow rate or to the amount required for cooling, and branching off a portion of it and introducing it into the adsorption inlet. To solve this problem, Figures 5c and 5e include a supplementary gas flow (dashed line) branching off from the cooling gas flow and joining the inlet gas flow.

[0123] This gas flow may be the reverse of the flow shown. Furthermore, outside air, exhaust gas from a pollutant source, or purified gas may be used in place of the above gas flow. Here, outside air may include clean atmospheric air, air with an adjusted oxygen concentration, or, if the combustible material is a gaseous substance, an inert gas such as non-reactive nitrogen, carbon dioxide, or helium. Figure 7c illustrates the use of purified gas as a supplementary gas flow.

[0124] Figure 11 is a schematic diagram illustrating a desorbed gas stream being recycled and passing through an oxidizer using a catalyst combined with a heating means.

[0125] Here, the first cooling gas stream recycled to the oxidizer has a high concentration of contaminants and a high temperature. At this time, if the concentration of contaminants is too high, the first cooling gas stream can be branched to form a bypass path that does not pass through the heating means and the oxidizer. In this case, the concentration within the recycled gas stream can be processed more stably, and in order to prevent the temperature of the gas stream oxidized by the oxidizer from rising too high, it is configured to be bypassed when the concentration exceeds a certain level. At this time, the oxidizer can be heated by the recycled desorption gas stream, the second cooling gas stream, and the outside air, so that the temperature at the rear end of the oxidizer can be controlled to not become too high. The bypass ratio is not particularly limited, but is preferably 50% or less.

[0126] The present invention is applicable to a device for concentrating and processing gaseous substances such as odors, carbon dioxide, and volatile organic compounds.

Claims

1. In an adsorption concentrator for adsorbing and concentrating gaseous substances in exhaust gas emitted from an emission source, and a concentration and oxidation device for oxidizing the gaseous substances concentrated by the adsorption concentrator, The above adsorption concentrator, An adsorption member including an adsorption region, a desorption region, and a cooling region for adsorbing and concentrating and desorbing gaseous substances in an exhaust gas emitted from an emission source; and A conduit providing a plurality of streams including an exhaust gas stream for introducing the exhaust gas from the exhaust source into the adsorption region, a desorption gas stream for introducing and discharging the desorption region, a cooling gas stream for introducing and discharging cooling gas into the cooling region, and a recirculation stream branching from the desorption gas stream discharged from the desorption region and joining at least one of the exhaust gas stream, the cooling gas stream, and the desorption gas stream; The above-mentioned concentrated oxidation device, A heating means for heating the desorption gas flow flowing into the desorption area, comprising an oxidizer for oxidizing the cooling gas stream or the gas branched from the cooling gas stream; The oxidizer exhaust gas stream oxidized and discharged from the above oxidizer flows into the desorption gas stream flowing into the above desorption area or joins the desorption gas stream flowing into the above desorption area. Concentrated oxidation device.

2. In paragraph 1, The cooling region of the above adsorption member includes a first cooling region and a second cooling region, and a gas flow passing through the first cooling region has a higher temperature than a gas flow passing through the second cooling region. The first cooling gas stream passing through the first cooling zone is introduced into the oxidizer. Concentrated oxidation device.

3. In paragraph 2, The above first cooling gas flow is introduced into the oxidizer through the heating means, Concentrated oxidation device.

4. In paragraph 1, a first oxidizer inlet gas stream branched from a first point of the above cooling gas stream and provided to the oxidizer; and comprising a first oxidizer exhaust gas stream discharged from said oxidizer and joining a second point of said cooling gas stream; The above first point is a point downstream of the gas flow path from the above second point. Concentrated oxidation device.

5. In paragraph 1, a first oxidizer inlet gas stream branched from a first point of the above cooling gas stream and provided to the oxidizer; and comprising a first oxidizer exhaust gas stream discharged from said oxidizer and joining a second point of said cooling gas stream; The above first point is an upstream point in the gas flow path than the above second point. Concentrated oxidation device.

6. In paragraph 1, A concentrated oxidation device, wherein the oxidizer is one selected from the group consisting of a catalytic oxidizer, a catalytic oxidizer with an indirect heat exchanger, a regenerative oxidizer, and a regenerative catalytic oxidizer.

7. In paragraph 1, A concentrated oxidation device in which the first oxidizer inlet gas stream is branched off from the rear end of the heating means.

8. In paragraph 1, A concentrated oxidation device, wherein the first oxidizer inlet gas stream is branched when the concentration of the desorption gas stream is greater than a preset concentration.

9. In paragraph 1, A concentrated oxidation device comprising a second oxidizer inlet gas stream branched from a desorption gas stream flowing into the desorption area and supplied to the oxidizer.

10. In paragraph 9, A concentrated oxidation device in which the purge gas passing through the above purge zone joins the cooling gas flow flowing out from the above cooling zone.

11. In paragraph 1 A concentrated oxidation device, wherein the above recirculation stream joins the cooling gas stream flowing into the above cooling zone.

12. In paragraph 1 A concentrated oxidation device in which the above recirculation stream joins the exhaust gas stream flowing into the above adsorption zone.

13. In paragraph 1, A concentrated oxidation device, wherein the above recirculating flow is provided with a cooling means or a condensation recovery means.

14. In paragraph 1, A concentrated oxidation device having a cooling means provided for the above desorption gas flow.

15. In paragraph 1, A concentrating and oxidizing device, wherein a portion of the above cooling gas stream joins the inlet gas stream.

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