Gaseous material concentration device and gaseous material treatment device comprising same

Abstract

The present invention relates to a gaseous material treatment device, which concentrates and desorbs a low-concentration gaseous material by means of a rotary rotor so as to condense, recover and remove same. The present invention provides the gaseous material concentration device comprising: an adsorption member having a plurality of functional areas for adsorbing and concentrating / desorbing a gaseous material in a discharge gas discharged from a discharge source; and a driving unit for rotating the adsorption member relative to the gaseous material, the functional areas of the adsorption member including an adsorption area, a desorption area, a primary cooling area and a secondary cooling area, wherein the concentration device comprises a discharge gas flow path allowing inflow from the discharge source to the adsorption area, a desorption gas flow path for discharging the concentrated gas from the desorption area, a first recirculation flow path branched from the desorption gas flow path so as to pass through the primary cooling area, and a secondary cooling gas flow path passing through the secondary cooling area, and a part of the concentrated gas in the desorption gas flow path is joined in the discharge gas flow path through a second recirculation flow path.

Description

Gaseous substance concentration device and gaseous substance processing device including the same

[0001] The present invention relates to a device for concentrating and processing gaseous substances such as odors, carbon dioxide, and volatile organic compounds, and more specifically, to a gaseous substance processing device for concentrating low-concentration gaseous substances discharged from air purifiers, printing processes, painting processes, semiconductor processes, carbon dioxide emission facilities, and odor facilities, and desorbing them by using a rotating rotor, condensing, recovering, and removing them.

[0002] As legal regulations on atmospheric environment are strengthened, it is becoming increasingly difficult to oxidize gaseous substances containing volatile organic compounds using heat or catalysts. Typically, these gases contain a small amount of combustible components, making oxidation systems utilizing high temperatures above 800°C or catalysts above 300°C uneconomical due to the high energy consumption. Therefore, regenerative thermal combustion, a recent technology that utilizes thermal storage media to recover heat at a rate of over 95%, is widely used to treat low-concentration volatile organic compounds. This process maintains an oxidation temperature above 800°C to oxidize volatile organic compounds at high temperatures. Generally, operation is possible without additional fuel when the temperature rise due to the oxidation calorific value of volatile organic compounds in the gaseous substance is 40-80°C per cubic meter of gas. However, when the temperature rise is below 40°C per cubic meter of gas, additional fuel is required. In the regenerative thermal combustion method, the regenerative thermal combustion method using a catalyst is called the regenerative catalytic combustion method, and since the combustion temperature can be lowered to 300-450℃, it is more economical to process. However, even in this case, if the calorific value per cubic meter of gas of the volatile organic compounds contained in the gaseous substance is less than 15-30℃, a lot of additional energy is consumed. In actual painting processes, gaseous substances containing odors and volatile organic compounds are often emitted in environments where low concentrations of volatile organic compounds are emitted due to high air volumes. Therefore, in order to combust and oxidize low concentrations of odors and volatile organic compounds, additional fuel must be added, and this has the disadvantage of high maintenance costs due to the high energy consumption.

[0003] As a method for processing existing low-concentration gaseous substances, Japanese Patent Application Laid-Open No. 1997-173758 provides a high-boiling-point solvent recovery device comprising a honeycomb structure rotor supporting an adsorbent, a separator dividing the vicinity of the cross-section of the rotor into two regions, an adsorption region and a desorption region, a blower supplying solvent-containing air having a boiling point of 150 to 300°C to the adsorption region, releasing a portion of the purification gas flowing out from the opposite cross-section of the rotor into the atmosphere and supplying the remainder to the desorption region, a heating means for heating the purification gas, a cooling means for separating the solvent-enriched gas into a liquefied recovery product and a cooled lean gas, and a return means for returning the cooled lean gas as a raw material. This device can concentrate by a concentration multiple of 5 to 15 times. In such a conventional adsorption concentration device, an adsorbent such as zeolite, activated carbon, or silica is coated on a honeycomb-shaped ceramic support, and the concentration multiple is determined by the adsorption amount of the substance.

[0004] Meanwhile, Korean Patent No. 2383095 provides a concentrating device for concentrating a gaseous substance, including an adsorption member forming a plurality of functional areas for adsorbing, concentrating, and desorbing pollutants in a gas, and a driving unit for relatively rotating the adsorption member with respect to the gaseous substance, wherein a portion of the concentrated gas in the desorption gas path flows into the adsorption region through the recirculation path. However, although this method has the advantage of concentrating the concentrated recirculated gas to a high concentration by introducing it into the adsorption region, thereby reducing the capacity of the post-treatment system, there is a concern that the efficiency may be lowered because more adsorption members are required to re-adsorb the pollutants concentrated to a high concentration, and there is a problem that additional energy is required to desorb the pollutants adsorbed to a high concentration.

[0005] In order to solve the problems of the above-mentioned prior art, the present invention aims to provide a gaseous substance treatment system capable of saving energy and effectively removing gaseous substances by concentrating gaseous substances to a high concentration from an emission source containing and emitting low-concentration gaseous substances and using the same in combustion, recovery, and condensation treatment means.

[0006] In addition, the present invention aims to provide a gaseous substance processing system that concentrates a gaseous substance to a high concentration while suppressing an increase in desorption energy by using a concentrating means composed of a plurality of functional regions including an adsorption region, a desorption region, and a cooling region.

[0007] In addition, the present invention aims to provide a gaseous substance processing system capable of concentrating a gaseous substance to a high concentration by minimizing re-adsorption in an adsorption region using a concentrating means composed of a plurality of functional regions including an adsorption region, a desorption region, and a cooling region.

[0008] In addition, the present invention aims to provide a gaseous substance processing system having a plurality of cooling zones as functional zones, thereby concentrating gaseous substances at a high concentration while suppressing an increase in desorption energy.

[0009] In addition, the present invention aims to provide a gaseous substance processing system capable of concentrating a gaseous substance to a high concentration by minimizing re-adsorption in an adsorption region by having a plurality of cooling regions as functional regions.

[0010] In addition, the purpose is to provide a gaseous substance treatment system that can stably supply the flow rate, concentration and temperature of the cooling stream, the flow rate and concentration of the desorption stream, and the energy required for desorption while appropriately controlling the recirculation rate required for high-concentration concentration and taking into consideration the safety and convenience of the operator.

[0011] In order to achieve the above technical task, the present invention provides a gaseous substance concentrating device including an adsorption member forming a plurality of functional regions for adsorbing and concentrating and desorbing gaseous substances in an exhaust gas discharged from an emission source, wherein the plurality of functional regions of the adsorption member include an adsorption region, a desorption region, a primary cooling region, and a secondary cooling region, and the concentrating device includes an exhaust gas path flowing into the adsorption region from the emission source, a desorption gas path discharging a concentrated gas from the desorption region, a first recirculation path branching from the desorption gas path and passing through the primary cooling region, and a secondary cooling gas path passing through the secondary cooling region, and wherein a portion of the concentrated gas in the desorption gas path flows into the primary cooling region through the first recirculation path.

[0012] At this time, a portion of the concentrated gas in the desorption gas path may join the exhaust gas path through the second recirculation path. Additionally, simultaneously or separately, a portion of the concentrated gas in the desorption gas path may join the desorption gas path flowing into the desorption area through the third recirculation path.

[0013] In the present invention, when the value obtained by dividing the concentrated gas flow rate branched into the recirculation path by the concentrated gas flow rate of the desorption gas path is referred to as the recirculation rate, the recirculation rate can be controlled according to the concentration of pollutant components in the exhaust gas flowing into the adsorption region.

[0014] In the present invention, a concentration sensor may be provided in at least one of the exhaust gas path, the desorption path, the recirculation path, and the exhaust path.

[0015] In the present invention, the recirculation rate can be controlled according to the concentration of the pollutant component measured by the concentration sensor.

[0016] In the present invention, the recycling rate may be 1 to 99.9%.

[0017] The present invention includes a desorption means for heating a desorption gas flow supplied to the desorption area, and a gas flow flowing through the recirculation gas path can be heated by the desorption means.

[0018] The present invention includes a desorption means for heating a desorption gas flow supplied to the desorption area, and a gas flow flowing through the secondary cooling gas path can be heated by the desorption means.

[0019] In the present invention, the gas flow flowing through the secondary cooling gas path may include external air, exhaust gas, or purified exhaust gas.

[0020] In the present invention, a cooling means may be provided in the desorption gas path.

[0021] In addition, the present invention further includes a concentrated gas treatment means, and the concentrated gas treatment means may be a condensation recovery device through cooling and pressurization, a concentration recovery device using an adsorbent and an absorbent, or an oxidation device that removes polluted gas through oxidation.

[0022] In the present invention, the treated gas recovered by the condensation recovery device can be supplied to the adsorption area or cooling area of ​​the adsorption member.

[0023] According to the present invention, a low-concentration gaseous substance is adsorbed using a concentrating means having a plurality of functional areas, and a portion of the desorbed concentrated gas is recycled using a heat source, thereby concentrating the low-concentration gaseous substance to a high concentration, and using this in a combustion, recovery and condensation treatment means, thereby enabling energy savings and effective removal of the gaseous substance.

[0024] According to the present invention, it is possible to minimize the increase in energy required for desorption even though a gaseous substance is concentrated by recycling a portion of the desorbed gas that is adsorbed and desorbed in the concentrating means.

[0025] In addition, according to the present invention, a portion of the high-concentration gas adsorbed and desorbed in the concentrating means is recycled, and the concentration rate of the gaseous substance is improved by concentrating it to a high concentration without re-adsorption in the adsorption region.

[0026] Accordingly, the concentration ratio can be increased by up to 300 times, minimizing the size of the final treatment means and allowing more economical treatment of gaseous substances.

[0027] FIG. 1 is a schematic drawing of a concentrating device for highly concentrating and processing a gaseous substance according to one embodiment of the present invention.

[0028] Figure 2 is a conceptual drawing illustrating that a cross-section of an adsorption member of a concentration device is divided into multiple functional areas.

[0029] FIG. 3 is a schematic diagram showing a first embodiment of a gaseous substance processing device according to one embodiment of the present invention.

[0030] FIG. 4 is a schematic diagram showing a second embodiment of a gaseous substance processing device according to one embodiment of the present invention.

[0031] FIG. 5 is a schematic diagram showing a third embodiment of a gaseous substance processing device according to one embodiment of the present invention.

[0032] FIG. 6 is a schematic diagram showing a fourth embodiment of a gaseous substance processing device according to one embodiment of the present invention.

[0033] The present invention will be described in detail with reference to the drawings below.

[0034] 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.

[0035] 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.

[0036] 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.

[0037]

[0038] FIG. 1 is a side view schematically illustrating a concentration device according to one embodiment of the present invention.

[0039] Referring to FIG. 1, the concentrator (100) may include an adsorption member (10 in FIG. 3) forming a plurality of functional areas for adsorbing and concentrating / desorbing a gaseous substance, and a driving unit for relatively rotating the adsorption member with respect to the gaseous substance.

[0040] The above-described concentrator (100) provides a plurality of gas paths. As illustrated, suitable paths are provided to provide, for example, an exhaust gas flow (①) from a pollutant (or emission source) penetrating the internal adsorption member, a desorption gas flow (③) that desorbs adsorbed gaseous substances, and a cooling gas flow (②) for cooling a region of the adsorption member that has been heated after desorption. In addition, suitable paths are provided so that a portion of the desorption gas flow (③) branches off as a recirculation flow (④) and joins the cooling gas flow (②), and another portion is discharged as an exhaust flow (⑤).

[0041] In the present invention, various sources may be used as the supply source (⑥) of the cooling gas. For example, outside air, exhaust gas from a pollutant, or purified gas may be used. Here, outside air may include clean atmospheric air, air with controlled oxygen concentration, or, in the case of combustible materials in the form of gases, inert gases such as non-reactive nitrogen, carbon dioxide, and helium.

[0042] In addition, in the present invention, the concentrator (100) may be provided with appropriate gaseous substance transfer means, sensors, gas inlets, gas outlets, and a housing. In addition, appropriate valves, ducts, and blower means for branching the recirculation flow and the exhaust flow may be provided. In addition, in the present invention, a plurality of passages penetrating the adsorption member are separated and / or partitioned by appropriate sealing means so that the gas flows therethrough 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 passage can be separated and partitioned.

[0043] Figure 2 conceptually illustrates that the adsorption zone (A), cooling zone (C), and desorption zone (D) of the concentration device are separated into compartments.

[0044] Meanwhile, as illustrated in Fig. 1, the cooling gas flow (②) that has passed through the cooling area (C) is further heated through the desorption means (200) and flows into the desorption area (D). The desorption means (200) of the present invention may be implemented as a part of the concentrating device (100) or may be implemented as a separate, separate component.

[0045] Figure 1 illustrates exemplary directions of gas flow in gas paths (①, ②, ③), but the present invention is not limited thereto. At least one of the gas flows in each path may have a direction opposite to that illustrated.

[0046] The concentrator of Fig. 1 can use a cylindrical adsorption member (10) as in Fig. 2 as an adsorption concentration means for a gaseous substance.

[0047] The above-described adsorption member (10) may be formed of an appropriate material having heat storage properties and gas adsorption properties. In general, the adsorption member may 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 plate folded. Of course, the present invention is not limited thereto, and the adsorption member (10) 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] 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.

[0049] 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, which are hydrophilic adsorbents that adsorb moisture well, and the rear end member may include, as a main component, a hydrophobic zeolite having a Si / Al molar ratio of 15 or more and a zeolite (USY, ZSM5, etc.) that adsorbs volatile organic compounds well while having a low relative adsorption capacity for moisture.

[0050] Figure 3 is a schematic drawing showing a cross-section of the adsorption member (10) of the present invention.

[0051] In the present invention, the plurality of regions may be defined as areas in a direction substantially perpendicular to the gas flow flowing through the paths (①, ②, ③) described with reference to FIG. 1. For example, the area of ​​the region may be defined by a cross-sectional area perpendicular to the axis of the concentrator.

[0052] The above multiple regions may include functional regions such as, for example, an adsorption region (12), a desorption region (14), and a cooling region (16, 18).

[0053] In the adsorption member of the present invention, the areas occupied by the adsorption region (12), desorption region (14), and cooling region (16, 18) can be appropriately defined. In general, the area of ​​the adsorption region (12) can preferably occupy 40% to 90% of the total area of ​​the adsorption member (10). Accordingly, the adsorption region (12) can have a larger area than the desorption region (14) or the cooling region (16, 18).

[0054] Additionally, the areas of the adsorption area (12) and the desorption area (14) may generally be configured to be the same, or the desorption area (14) may be designed to have the same area as the cooling area (16, 18), or the desorption area (14) may be designed to be smaller than the cooling area (16, 18), and vice versa.

[0055] However, if the desorption area is larger than the cooling area and the cooling area is too small, the adsorption efficiency may be reduced due to the uncooled temperature in the subsequent adsorption area, and the recovery of energy applied to the desorption area may be reduced, which may increase the energy required for the desorption means to heat the cooling gas flow passing through the cooling area.

[0056] Below, a driving method for increasing heat energy recovery is described, but the present invention is not limited thereto and can be appropriately adjusted depending on the driving environment.

[0057] Preferably, the present invention may have a relationship of adsorption area > cooling area ≥ desorption area. Specifically, the cooling area / desorption area ratio in the present invention 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.

[0058] In Fig. 3, the cooling area is illustrated as being divided into a primary cooling area (16) and a secondary cooling area (18).

[0059] In the present invention, both the primary and secondary cooling zones perform a cooling function. The separation of the cooling zones in the present invention utilizes the temperature difference between the gases passing through each cooling zone. The gas flow passing through the primary cooling zone has a relatively higher temperature than the gas flow passing through the secondary cooling zone.

[0060] In addition, it goes without saying that the secondary cooling zone in the present invention can also perform a purge function. If the recirculation rate increases or the temperature and concentration of the concentrated gas coming from the desorption zone increase, it can be purged, and a zone for cooling or recovering the heat of the adsorption member may be required. For this purpose, a secondary cooling zone may be added. At this time, the cooling gas introduced into the secondary cooling zone may be one type of gas selected from outside air, exhaust gas, and purified exhaust gas, or a mixture thereof. Here, the outside air may include clean atmospheric air, air with adjusted oxygen concentration, and, if the combustible material is a gaseous substance, an inert gas such as non-reactive nitrogen, carbon dioxide, and helium.

[0061] In the present invention, when the adsorption member (10) is in operation, the adsorption member (10) functions as a plurality of regions, such as an adsorption region (12), a desorption region (14), a primary cooling region (16), and a secondary cooling region (18), and these regions can be isolated or separated by a sealing means.

[0062] FIG. 2 is a side view schematically illustrating a concentrating device according to another embodiment of the present invention including a two-stage cooling region.

[0063] Unlike Fig. 1, the concentrator (100) is provided with an appropriate flow path for the secondary cooling gas flow (⑦) that flows separately to the secondary cooling region (C2). The secondary cooling gas flow (⑦) that has passed through the adsorption member (10) may flow in a separate flow path separated from the primary cooling gas flow (②). Alternatively, the secondary cooling gas flow (⑦) that has passed through the adsorption member (10) may of course merge with the primary cooling gas flow (②) that has passed through the adsorption member. The desorption means may be installed on the flow path in which the primary cooling gas flow (②) is present, and the desorption means (200) may be installed at any position before or after the primary cooling gas flow (②) and the secondary cooling gas flow (⑦) merge.

[0064] The secondary cooling gas flow (⑦) is branched off from the exhaust gas flow (①) and flows into the secondary cooling region (C2), but the present invention is not limited thereto. External air or purified gas may be used as the secondary cooling gas flow. The gas flow passing through the secondary cooling gas region (C2) may flow into the desorption means (200) and join with the primary cooling gas flow (②). Alternatively, part or all of the secondary cooling gas flow (⑦) may be supplied to a location other than the desorption means (200).

[0065] FIG. 4 is a schematic diagram illustrating an example of a gaseous substance treatment device for highly concentrating gaseous substances from a low-concentration gaseous substance emission source according to one embodiment of the present invention.

[0066] Referring to FIG. 4, the gaseous substance treatment device includes a concentration device (100), a desorption means (200), and a concentrated gas treatment means (300).

[0067] Referring to FIG. 4, pollutants or harmful components, that is, gaseous substances, contained in the exhaust gas flowing in from the emission source are adsorbed on the adsorbent of the adsorption member (10) of the concentrator (100) while passing through the concentrator (100). The concentrator (100) is preferably a rotor-type adsorption and concentration means capable of controlling the rotational speed according to the concentration of the gaseous substances flowing in. In the present embodiment, the concentrator (100) can rotate at a rotational speed of 2 to 20 rph. In the present invention, the rotational speed of the concentrator is exemplary and may be set differently according to process conditions or process conditions. In addition, the operation method of the rotor type is such that adsorption, cooling, and desorption are repeatedly performed, and the rotation method of the rotor is not limited to whether it is continuous or intermittent.

[0068] As described above, the gaseous substance contained in the exhaust gas of the emission source flows into the concentrator (100) and is adsorbed on the adsorbent member (10) in the adsorption area (A). As the rotor rotates, the adsorbent member (10) that has adsorbed the gaseous substance enters the desorption area (D) and is desorbed by the desorption air. At this time, the desorption gas is used at a lower flow rate than the exhaust gas flowing into the adsorption area. 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 of gaseous substance 3 to 30 times that of the adsorbed gas. The flow rate of the exhaust gas flowing into the adsorption area 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 substance cannot be delivered, and thus desorption will not occur. Therefore, it must be appropriately adjusted.

[0069] Meanwhile, in the present invention, the exhaust gas from the emission source can be used as a cooling gas. In this case, as illustrated, a portion of the exhaust gas from the emission source branches off from the exhaust gas flow (①), passes through the secondary cooling region (C2), and joins the first cooling gas flow (②). At this time, the joining point of the secondary cooling gas flow (⑦) may be upstream or downstream of the desorption means (200). The ratio of the flow of the second cooling gas (⑦) branched off from the exhaust gas flow (①) determines the content of pollutant components in the desorbed gas, and thus this ratio can regulate the concentration multiple. For example, the ratio of the exhaust gas used as a 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. It is generally used mainly in the field at 3 to 30 times, 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.

[0070] The concentration device of the present invention comprises a desorption means (200) for heating the desorption gas. In the present invention, the desorption means (200) 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 desorption 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 desorption gas flow or transferring heat energy through an indirect heat exchanger may be used.

[0071] As previously described with reference to Figure 1, a portion of the desorbed gas is branched off and rejoins the cooling gas flow. This branching mechanism may consist of a duct and a valve.

[0072] Fig. 4 illustrates an exhaust duct (120) and a recirculation duct (130) as an example of a branching mechanism for desorption gas. In the present invention, the exhaust duct (120) and the recirculation duct (130) may be equipped with a flow control means such as a valve.

[0073] In the present invention, the first cooling gas flow (②) passing through the recirculation duct (130) is concentrated compared to the exhaust gas flow (①) and includes a gaseous substance having a high concentration. In the present invention, the concentration concentration can be determined according to the concentration multiplier 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 (see Table 2 below), 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.

[0074]

[0075] The first cooling gas flow (②) is heated by a desorption means (200) alone or combined with a second cooling gas flow (⑦) and flows into the desorption area (B) of the adsorption member (10) to desorb the adsorbed pollutants, thereby concentrating the desorbed gas flow (③). In this way, the concentration of pollutants in the exhaust gas recirculation flow (④), the first 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 operator, i.e., an equilibrium concentration.

[0076] 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.

[0077] 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.

[0078] Meanwhile, in order to use the desorption gas as a recirculating flow in the present invention, part or all of the desorption gas may be heat exchanged.

[0079]

[0080] 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 subjected to the sequence of adsorption → desorption → cooling 1 → cooling 2 → adsorption → desorption → cooling 1 → cooling 2, so that the exhaust gas flow can be gradually concentrated into a high-concentration gaseous substance.

[0081] In the present invention, the concentration of the circulated exhaust gas is higher than the concentration of the inflowing gas, and the temperature and concentration of the cooling gas are higher than in the case where it is not circulated due to heat transfer during the desorption process. At this time, the exhaust gas with high concentration remains in the adsorption member and when it moves to the adsorption area, it may escape immediately without being adsorbed in the adsorption area. Although the effect of this is not large, a purge section that does not include the circulated exhaust gas can be additionally provided to eliminate the effect and lower the temperature. For example, a certain area of ​​the adsorption member (10) in contact with the secondary cooling area (C2) of the concentrator (100) illustrated in FIGS. 2 and 3 can be set as a purge area. The purge air used at this time can be used by injecting external air, exhaust gas from the emission source, or purified gas for purging. Here, the external air may include clean atmospheric air, air with adjusted oxygen concentration, or, if the combustible material is a gaseous substance, an inert gas such as non-reactive nitrogen, carbon dioxide, and helium.

[0082]

[0083] In this case, the gas streams passing through the cooling zone and the purge zone can be separated or combined. Since the gases passing through the cooling zone and the purge zone can be mixed and heated by a heating means and then introduced into the desorption zone, they do not necessarily need to be separated into separate compartments. In other words, since the gas passing through the purge zone contains gaseous substances, there are several methods for sending it as a desorption stream, sending it to an adsorption zone, or sending it directly to a final processing device for gaseous substances, but sending it as a desorption stream is the most preferable method.

[0084] 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.

[0085] In the present invention, the concentration ratio of gaseous substances 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 gaseous substances 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.

[0086] For example, the concentration of gaseous substances 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 vapor that can explode is not constant, and to maintain 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.

[0087] The device of the present invention may be equipped with a concentration sensor (150) for measuring the concentration of gaseous substances in order to control the recirculation rate. In Fig. 3, 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 (160) may be installed on the gas flow path passing through the adsorption member. This downstream concentration sensor (160) is for controlling the adsorption efficiency so that the concentration at the downstream of the adsorption member does not increase above a certain level.

[0088] Referring again to FIG. 4, the concentrated gas treatment means (300) may be a condensation recovery device through cooling and pressurization, a second concentration recovery device using an adsorbent and an absorbent, or an oxidation device such as an RTO, RCO, or TO that removes polluted gases through combustion. In addition, when a condensation recovery device is used in the present invention, the primary treated gas recovered by the condensation recovery device may be supplied again to the adsorption area or cooling area of ​​the adsorption member to perform additional purification.

[0089]

[0090] In the concentration device of Fig. 1, the concentration multiple is fixed at 12 times, and the concentration of the pollutant component according to the recirculation rate (equilibrium concentration, g / Nm 3 ) is calculated as shown in Table 1 below (concentration multiple 12 times). At this time, the inlet concentration of the exhaust gas stream emitted from the emission source containing oxygen is changed to 0.25 to 1.0 g / Nm3, and the concentration of pollutants according to the recirculation rate (g / Nm 3) was calculated. The concentration of the pollutant was calculated as the saturation concentration when repeated several times. Toluene was assumed as the pollutant, the LEL was 1.27%, and the stability standard was 1 / 4 of the LEL. The temperature effect of the LEL was ignored. In addition, the treatment rate was assumed to be 95%. In Table 1 below, the left column shows the recirculation rate (%), and the right row shows the inlet concentration (g / Nm 3 ) is indicated.

[0091]

[0092] Classification 0.250.50.75195%57.013114.025171.038228.05080%14.26328.52542.78857.05060%7.13814.27521.41328.55040%4.7639.52514.28819.05020%3.5757.15010.72514.3005%3.0136.0259.03812.0500%2.8635.7258.58811.450

[0093] From the table above, it can be seen that the equilibrium concentration of toluene gradually increases as the recirculation rate increases from 0 to 95%. Meanwhile, when the concentration ratios are 15 times and 6 times, respectively, and the remaining conditions are the same, the results of calculating the equilibrium concentration are as shown in Table 2 (concentration ratio 15 times) and Table 3 (concentration ratio 6 times) below.

[0094] Classification 0.25 0.5 0.75 195% 71.26 21 42.5 25 21 3.78 8 28 5.05 0 80% 17.8 25 35 65 0 53.47 57 1.30 0 60% 8.9 19 17.83 8 26.75 635 67 5 40% 5.9 5 0 11.9 0 17.85 0 23.80 0 20% 4.46 68 93 113.39 7 17.86 35% 3.76 37.5 25 11.28 8 15.05 00% 3.57 5 7.15 0 10.72 5 14.300

[0095] Classification 0.511.5295%57.025114.050171.075228.10080%14.27528.55042.82557.10060%7.15014.30021.45028.60040%4.7759.55014.32519.10020%3.5887.17510.76314.3505%3.0256.0509.07512.1000%2.8755.7508.62511.500

[0096] FIG. 5 is a drawing illustrating a second embodiment having a branching mechanism for desorption gas. Referring to FIG. 5, in addition to the exhaust duct (120) and the first recirculation duct (130A) described with reference to FIG. 4, a second recirculation duct (130B) is provided. In the present invention, the exhaust duct (120) and the recirculation ducts (130A, 130B) may be equipped with flow control means such as a valve or a blower.

[0097] The above second recirculation duct (130B) may be directly branched from the desorption gas flow (③) or branched again from the branched first recirculation duct (130A), and the number of installations is not limited. In addition, the second exhaust gas recirculation flow (⑧) may be joined at a position before or after the secondary cooling gas flow (⑦) branches from the exhaust gas flow (①). If the secondary cooling gas flow is joined after the branch, there is an advantage in that the temperature and concentration of the gas flowing into the secondary cooling region can be controlled to be lower.

[0098] In the present invention, the second exhaust gas recirculation stream (⑧) passing through the second recirculation duct (130B) includes 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 flow rate ratio of the concentrated drainage and the recirculated concentrated gas. In addition, the concentration concentration can also be determined by the ratio of the first exhaust gas recirculation stream (④) and the second exhaust gas recirculation stream (⑧). When the second exhaust gas recirculation stream (⑧) is installed as in the present embodiment, the amount of gas flow supplied to the final treatment means can be adjusted, thereby having the advantage of stably maintaining the treatment capacity of the final treatment means, and can prevent the concentration of the gas flowing into the desorption means (200) from becoming excessively high.

[0099] In this embodiment, a portion of the exhaust gas recirculation stream (④) joins the exhaust gas stream (①), and another portion joins the cooling gas stream (②), thereby increasing the concentration of pollutants in the desorbed gas. By repeating adsorption, cooling, and desorption, the concentration of pollutants in the first exhaust gas recirculation stream (④), the second exhaust gas recirculation stream (⑧), the first cooling gas stream (②), and the desorbed gas stream (③) increases, and after several repetitions, reaches a certain concentration selected by the operator, i.e., an equilibrium concentration.

[0100]

[0101] Figure 6 is a drawing showing a third embodiment having a branching mechanism for desorption gas.

[0102] Referring to Fig. 6, in addition to the exhaust duct (120) and the first recirculation duct (130A) described with reference to Fig. 4, a third recirculation duct (130C) is provided. In the present invention, the exhaust duct (120) and the recirculation ducts (130A, 130C) may be provided with a flow control means such as a valve, a blower, etc.

[0103] In the present invention, the third exhaust gas recirculation stream (⑨) passing through the third recirculation duct (130C) is concentrated compared to the exhaust gas stream (①) and contains a gaseous substance with a high concentration. In the present invention, the concentration can be determined according to the flow rate of the concentrated drainage and the concentrated gas to be recirculated. In addition, the concentration can also be determined by the ratio of the first exhaust gas recirculation stream (②) and the third exhaust gas recirculation stream (⑨).

[0104] When the third exhaust gas recirculation flow (⑨) is used as in this embodiment, the temperature rise of the cooling gas flow can be controlled, as in the embodiment of FIG. 4, and desorption energy can be added by increasing the amount of desorption gas, which has the advantage of being advantageous for desorption. The third recirculation duct (130C) can be installed at any position in the gas flow path from the outlet of the cooling zone to the inlet of the desorption zone, but it is preferably installed in front of the desorption means (200). In addition, when an external high-temperature air (waste heat or heated air) flow is brought in as desorption air, the third exhaust gas recirculation flow (⑨) can be supplied mixed with the high-temperature air flow.

[0105] The third exhaust gas recirculation flow (⑨) joins the first cooling gas flow (②) and the second cooling gas flow (⑦) and flows into the desorption area (B) of the adsorption member (10) to desorb the adsorbed gas, thereby making the desorbed gas flow (③) more concentrated. Meanwhile, the concentration of pollutants in the first cooling gas flow (②), the third exhaust gas recirculation flow (⑨), 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.

[0106]

[0107] Fig. 7 is a drawing showing a fourth embodiment having a branching mechanism for desorption gas.

[0108] Referring to Fig. 7, it can be seen that the exhaust duct (120) and the first recirculation duct (130A) described with reference to Fig. 4 are combined with a second recirculation duct (130B) and a third recirculation duct (130C). In the case of this embodiment, it can have the advantage of being able to appropriately control the temperature of the cooling gas flow, stably maintain the flow rate of the final treatment means, and stably provide the desorption energy required for desorption.

[0109]

[0110] Meanwhile, although FIGS. 5 to 7 illustrate that the second exhaust gas recirculation flow and / or the third exhaust gas recirculation flow coexist with the first exhaust gas recirculation flow, the second exhaust gas recirculation flow or the third exhaust gas recirculation flow may be provided without the first exhaust gas recirculation flow. Furthermore, the present invention may provide two or more of the first exhaust gas recirculation flow, the second exhaust gas recirculation flow, and the third exhaust gas recirculation flow as recirculation flows.

[0111]

[0112] 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. A concentrating device for concentrating a gaseous substance, including an adsorption member forming a plurality of functional areas for adsorbing, concentrating and desorbing gaseous substances in an exhaust gas emitted from an emission source, The multiple functional regions of the above adsorption member include an adsorption region, a desorption region, a primary cooling region, and a secondary cooling region, The above-mentioned concentration device, It includes an exhaust gas path flowing from the above emission source into the above adsorption region, a desorption gas path discharging a concentrated gas from the above desorption region, a first recirculation path branching from the desorption gas path and passing through the first cooling region, and a second cooling gas path passing through the second cooling region. A gaseous substance concentration device, characterized in that a portion of the concentrated gas of the above desorption gas path flows into the first cooling area through the first recirculation path.

2. In paragraph 1, A gaseous substance concentration device, characterized in that a portion of the concentrated gas of the above-desorbed gas path joins the above-desorbed gas path through a second recirculation path.

3. In paragraph 1 or 2, A gaseous substance concentration device, characterized in that a portion of the concentrated gas of the above desorption gas path joins the desorption gas path which flows into the desorption area through the third recirculation path.

4. In paragraph 1, When the value obtained by dividing the flow rate of concentrated gas branched into the above recirculation path by the flow rate of concentrated gas of the above desorption gas path is called the recirculation rate, A gaseous substance concentration device, characterized in that the above recirculation rate is controlled according to the concentration of pollutant components in the exhaust gas flowing into the above adsorption region.

5. In paragraph 4, A gaseous substance concentration device characterized in that a concentration sensor is provided in at least one of the exhaust gas path, the desorption path, the recirculation path, and the exhaust path.

6. In paragraph 5, A gaseous substance concentration device, characterized in that the above recirculation rate is controlled according to the concentration of the pollutant component measured by the concentration sensor.

7. In paragraph 4, A gaseous substance concentration device characterized in that the above recycling rate is 1 to 99.9%.

8. In paragraph 1, Comprising a desorption means for heating a desorption gas flow supplied to the above desorption area, A gaseous substance concentrator, characterized in that the above-mentioned desorption means heats the gas flow flowing through the above-mentioned recirculating gas path.

9. In paragraph 1, Comprising a desorption means for heating a desorption gas flow supplied to the above desorption area, A gaseous substance concentrator, characterized in that the above-mentioned desorption means heats the gas flow flowing through the second cooling gas path.

10. In paragraph 1, A gaseous substance concentration device, characterized in that the gas flow flowing through the secondary cooling gas path includes outside air, exhaust gas, or purified exhaust gas.

11. In paragraph 1, A gaseous substance concentration device characterized in that a cooling means is provided in the above desorption gas path.

12. In paragraph 1, Further comprising a means for processing concentrated gas, A gaseous substance concentration device characterized in that the above-mentioned concentrated gas treatment means is a condensation recovery device through cooling and pressurization, a concentration recovery device using an adsorbent and an absorbent, or an oxidation device that removes polluted gas through oxidation.

13. In paragraph 12, A gaseous substance concentration device characterized in that the treated gas recovered by the above condensation recovery device is supplied to an adsorption area or cooling area of ​​an adsorption member.

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