KR102525754B1 - Voc concentrating system convertible of batch type - Google Patents

Abstract

The present disclosure relates to a concentrator concentrating volatile organic compounds (VOCs) including ketones, alcohols, aromatic compounds, olefins, etc., from emitted gases (exhaust gas), and a method and system operating the same. Specifically, a technology included in the present invention is an environmental technology for improving air quality by treating various VOCs generated in factories. According to the method and system in the present disclosure, a reliable and safe means capable of maintaining ventilation for a production process in a discontinuous state is provided to maintain a low emitting process or a working space environment without fuel consumption. In addition, according to the method and system in the present disclosure, since the concentrator serves like an activated carbon tower, a legal emitting amount is complied, and a highly economic air pollution reduction system can be operated regardless of whether there is a discontinuous production process and there is any concentration plan across the shipbuilding, automobiles, and automobile parts fields.

Description

Batch type convertible volatile organic compound concentration system {VOC CONCENTRATING SYSTEM CONVERTIBLE OF BATCH TYPE}

This disclosure relates to a concentrator that concentrates organic compounds such as volatile organic compounds (VOCs), such as ketones, alcohols, aromatics, and olefins, from exhaust gas (exhaust gas), and methods and systems for operating the same. Specifically, the technical field to which the present invention belongs corresponds to environmental technology for improving air quality by treating various volatile organic compounds generated in factories.

Various prior technologies for removing volatile organic compounds (VOCs) emitted from industrial production facilities include thermal oxidation, catalytic oxidation, microwave decomposition, adsorption, and the like.

Recently, a process using an adsorption method together with a thermal oxidation method or a catalytic oxidation method has been widely spread. Adsorption methods, that is, technologies using a disk concentrator, such as a zeolite disk concentrator among the prior arts for adsorption and concentration, have limited adsorption capacity and safety during the desorption period. Due to the problem, it is generally used for continuous operation. Most production lines that do not operate 24 hours a day require special types of operating technology, such as batch and continuous type convertible systems for adsorption and desorption of volatile organic compounds.

1 is a conceptual schematic diagram of discontinuous production in general in the prior art. Referring to FIG. 1, a relatively high value among the concentration of volatile organic compounds in ppm (100), the highest concentration of volatile organic compounds at the time of emission (101), the concentration of volatile organic compounds after production time (102), and the upper limit of legal emissions ( bb, 103), a relatively low value (aa, 104) among the legal upper limits of emissions are shown, and the axis of fuel consumption (200) and maximum fuel consumption (202) are also shown. Regarding the operation time 300 corresponding to the horizontal axis of FIG. 1, a normal production period 301, an idle or standby period/time 302, a preparation/heating time 401, a normal operation period 402, and a rest period. Alternatively, a production standby period 403, a production stop/system shutdown period 404, an idle or standby period/batch mode operation period 405 are shown.

However, simply applying the prior art to such general discontinuous production causes various problems.

First, referring to Korean Patent Registration No. 10-0623498, which discloses activated carbon and a batch type reactor that can be used for a long time, activated carbon with improved adsorption capacity is used, and only for a limited period of time and a limited small flow rate. However, there is a disadvantage that it is difficult to function as a continuous concentration system.

In addition, referring to Korean Patent Registration No. 10-1343330, which uses a separated inert gas circulation to derive a high concentration ratio, the disclosed concentrator system performs a gas separation process without mixing with minimal oxygen. In spite of being used, there is a limitation in not suggesting a special solution in the case of discontinuous discharge.

In addition, Korean Patent Registration No. 10-0834800, which discloses an concentrator system using a honeycomb disk containing a catalyst for a catalytic reaction performed simultaneously with adsorption, also suggests a solution that can switch between operating modes, that is, a convertible mode solution. There is not.

Even in actual industrial sites, in a specific project of Novem Car Interiors (China) Co., Ltd., the present inventors have experienced adsorption and desorption using multi-boxed activated carbon, but However, it is larger than a single disc type concentrator and has the disadvantage of being vulnerable to fire, and has limitations in that it is impossible to perform high-rate enrichment.

In another project that supplied a concentration system employing a regenerative thermal oxidizer (RTO), the present inventors found that the facilities are economically economical during idle or standby periods due to the lack of system configuration that can maximize economic feasibility while satisfying emission regulations. It was confirmed that it is difficult to operate in an in-line manner.

In short, conventional concentrating systems with regenerative oxidizers cannot provide a function capable of switching between operating modes such as a batch mode and a continuous mode, so there is a problem in that fuel consumption is not reduced.

(Patent Document 1) KR 10-0623498 B

(Patent Document 2) KR 10-1343330 B

(Patent Document 3) KR 10-0834800 B

Accordingly, the present disclosure aims to solve the aforementioned problems of prior art enrichment systems by providing special hardware and operating logic enabling economical operation of the enrichment system.

In addition, in presenting specific hardware and operation logic, the purpose is to present a plan that can satisfy safety and stability as well.

The characteristic configuration of the present invention for achieving the object of the present invention as described above and realizing the characteristic effects of the present invention described later is as follows.

According to one aspect of the present disclosure, a system for concentrating volatile organic compounds is provided, wherein the system for concentrating volatile organic compounds adsorbs volatile organic compounds contained in the first exhaust gas 41 A concentrator (1) comprising an adsorption structure including an adsorbent for adsorption treatment of the volatile organic compound, and an actuator for driving the structure, wherein the concentrator (1) includes the A condenser ( One); a post-adsorption treatment gas conduit connected to the concentrator 1 and discharging the gas after adsorption treatment 16 from the concentrator 1; An air fan (3) for the concentrator generating a pressure gradient upstream or downstream of the concentrator (1) to transport the gas (16) after adsorption treatment from the concentrator (1) in a direction toward the gas conduit after treatment for adsorption (16). ; a desorption air supply conduit connected to the concentrator 1 and supplying desorption air 15 for desorbing the volatile organic compound from the adsorbent to the concentrator 1; a desorption air downstream conduit connected to the concentrator 1 and through which the desorption air 15 discharged from the concentrator 1 passes after the desorption treatment for the adsorbent by the desorption air 15 passes; Oxidizing a mixed gas (8) formed by mixing at least one second exhaust gas (42) containing a volatile organic compound with the desorption air (15) supplied through the desorption air downstream conduit at a predetermined joining point. As an oxidizer (2), the combustible gas (22) is supplied with combustion air (23) containing oxygen and a combustible gas (22), thereby combusting the volatile organic compounds contained in the mixed gas (8) together. an oxidizer (2) including a burner (24) for processing, wherein gas (27) after combustion processing generated in the combustion processing is discharged from the oxidizer (2); an oxidizer air fan (4) generating a pressure gradient for supplying the mixed gas (8) to the oxidizer (2); a combustion air fan generating a pressure gradient supplying the combustion air (23) to the oxidizer (2); and a heat supply means for supplying heat to the desorption air (15).

According to one aspect of the present disclosure, a switchable method of operation of a volatile organic compound enrichment system is provided, wherein the method includes an initial step of starting operation of the oxidizer 2 or starting a batch mode depending on a selected mode of operation. set point (initial set point; S410); a purging process (S420) of purging the oxidizer 2; a heating (preheating) step of heating (preheating) the oxidizer 2 (S430); a stand-by step (S440) of putting the oxidizer 2 on stand-by; a cleaning process (S450) of removing the volatile organic compounds using the concentrator 1 and the oxidizer 2; and a shutdown process (S460, S470) of shutting down the volatile organic compound concentration system.

According to the method and system of the present disclosure, a reliable and safe means to maintain ventilation for a production process in a discontinuous state is provided, thereby maintaining a low-emissions process or a production process with no fuel consumption. In addition, according to the method and system of the present disclosure, the concentrator can function like an activated carbon tower to comply with legal emissions, regardless of whether there is a discontinuous production process, not only in the field of shipbuilding, automobiles and automobile parts, but also in general industrial sites. In this case, a highly economical air pollution abatement system can be operated with or without a separate enrichment plan.

The inventors have been able to confirm that dramatic economics in fuel consumption are achieved by practical testing of the solution of the present disclosure.

For an understanding of the present invention, embodiments will be described with reference to the accompanying drawings in order to show the convertible method and system for a concentrator shown in this disclosure, which are only non-limiting examples, and the technical field to which this disclosure belongs Of course, other drawings may be obtained based on these drawings without additional effort leading to another invention for a person skilled in the art (hereinafter referred to as "the skilled person").
1 is a conceptual profile for the general incontiguous production in the prior art.
2 is a diagram showing a connection process diagram of a volatile organic compound concentration system according to the present disclosure by way of example.
3 is a flowchart exemplarily showing an operation sequence according to a conventional operating method of the volatile organic compound concentration system of the present disclosure.
4 is a flowchart exemplarily showing an operating sequence according to a switchable operating method of the volatile organic compound concentration system of the present disclosure.
5 is an exemplary diagram showing a comparison between fuel consumption of a volatile organic compound enrichment system according to a switchable operating method according to the present disclosure and fuel consumption according to a conventional operating method.
6 is an exemplary diagram showing a comparison between electricity consumption of a volatile organic compound concentration system according to a switchable operation method according to the present disclosure and electricity consumption according to a conventional operation method.
7 is an illustrative diagram showing temperature profiles inside the combustion chamber of an oxidizer employed in a volatile organic compound enrichment system according to the present disclosure for different days.
FIG. 8 is a diagram showing exemplarily the temperature profile inside the combustion chamber of the oxidizer employed in the volatile organic compound enrichment system according to the comparative example for different days.
9 is an exemplary diagram illustrating a temperature profile inside the combustion chamber of an oxidizer employed in a volatile organic compound enrichment system according to the present disclosure for normal operating days.
10 is a diagram showing an exemplary temperature profile according to a long-term test inside a combustion chamber of an oxidizer employed in a volatile organic compound enrichment system according to the present disclosure.

Unless defined otherwise, all terms used in this disclosure, including technical or scientific terms, have the same meaning as commonly understood by one of ordinary skill in the art. Terms such as those defined in commonly used dictionaries should be interpreted as having a meaning consistent with the meaning in the context of the related art, and unless explicitly defined in this specification, it should not be interpreted in an ideal or excessively formal meaning. don't

The following detailed description of the construction principle of the volatile organic compound concentration system according to the present disclosure and the switchable operating method therefor is intended to clarify the objects, technical solutions and advantages of the present disclosure presented in the present disclosure. Reference is made to the accompanying drawings which illustrate, by way of example, specific embodiments in which this may be practiced. In the description with reference to the accompanying drawings, the same reference numerals are given to the same components regardless of reference numerals, and overlapping descriptions thereof will be omitted. It will be appreciated that the structure of the structure inspection device according to the present disclosure does not have a length ratio as shown in the drawings, and the dimensions of each part in the drawings are only shown for purposes of explanation without limiting the scope of the present invention. . For example, the dimensions of some of the elements shown in the drawings are to aid understanding of various embodiments. In addition, the description and drawings are not meant to be written in the order in which they are written. Those skilled in the art will appreciate that acts and/or steps described or illustrated in a particular order may require no particular limitation to such order.

Accordingly, specific structural or functional descriptions of the embodiments are disclosed for illustrative purposes only, and may be modified and implemented in various forms.

And although terms such as first or second may be used to describe various components, these terms should be interpreted only for the purpose of distinguishing one component from another. For example, a first element may be termed a second element, and similarly, a second element may be termed a first element.

It should be understood that when an element is referred to as being “connected” to another element, it may be directly connected or connected to the other element, but other elements may exist in the middle. In addition, it should be understood that when an element is referred to as being 'on' another element, it may be 'directly on' the other element, but another element may exist in the middle.

Singular expressions include plural expressions and vice versa, unless the context clearly dictates otherwise.

In the present disclosure, the expression disposed "on", the expression disposed "on", and the expression disposed "between", unless otherwise specified, are arranged to be in direct contact with each other or interposed therebetween. It means that it was so arranged indirectly through other components. Moreover, "on ~" and "on ~" merely represent relative positions of components, because they may be seen differently depending on an observer's point of view. In addition, being formed "on (on)" has a broad meaning, and the fact that a component is formed on another component does not always mean a direct physical contact of a component to the other component.

In this disclosure, "upstream" expressed in relation to a path along which a pressure gradient is generated is a term referring to a location of relatively high pressure, and "downstream" refers to a location of relatively low pressure. As the term refers to, it will be understood that the fluid in a system in which an artificial pressure gradient is formed by a blower or the like flows from downstream to upstream in a corresponding path.

Moreover, the present invention covers all possible combinations of the embodiments presented herein. It should be understood that the various embodiments of the present invention are different, but need not be mutually exclusive. For example, specific shapes, structures, and characteristics described herein may be implemented in one embodiment in another embodiment without departing from the spirit and scope of the invention. That is, the embodiments of the present invention are described with reference to specific drawings of ideal embodiments of the present invention, but should not be considered as being limited to a specific shape as shown, and various modifications may be included. The shapes shown in the drawings are conceptually shown, and are not intended to limit the scope of the present invention by limiting the precise shape of a structure or region. For example, a region shown as a rectangle, square, etc. in the drawings may be variously deformed in shape, such as being tapered, curved, or rounded.

It should be understood that the location or arrangement of individual components within each disclosed embodiment may be changed without departing from the spirit and scope of the invention. Accordingly, the detailed description set forth below is not to be taken in a limiting sense, and the scope of the present invention, if properly described, is limited only by the appended claims, along with all equivalents as claimed by those claims.

In addition, in describing the present invention, if it is determined that the detailed description of a related known configuration or function is related to materials, processes, etc. well known to those skilled in the art and may obscure the gist of the present invention, it is excessively concerned. Detailed descriptions are omitted.

2 is a diagram showing a connection process diagram of a volatile organic compound concentration system according to the present disclosure by way of example.

In FIG. 2, the concentrator 1 is composed of a structure including an adsorbent and an actuator that drives the structure. For example, the structure has a cylindrical shape such as a disk or a polyhedron. It may have a shape, and the actuator may be a means for driving the structure to change the flow path, for example, a rotor that rotates the structure or a plurality of dampers that change the flow path without the structure being driven.

The concentrator 1 may be, preferably, a disk-type concentrator 1 having a honeycomb structure impregnated with zeolite, but is not limited thereto. In addition, the adsorbent may include one or more of zeolite, activated carbon, carbon fiber, and gamma-alumina (gamma-Al ₂ O ₃ ), but is not limited to such components and compositions, and its shape is porous, honeycomb, and bead-like. or amorphous, but not limited to such a form.

Referring to FIG. 2 , the first exhaust gas 41 is introduced into the concentrator 1 . The first discharge gas 41 is mainly for adsorption by the concentrator 1, that is, for concentration.

For example, the intake may be made by a pressure gradient generated by the operation of the air fan 3 for the concentrator. Preferably, before the first off-gas 41 enters the concentrator 1, a pre-treatment device, for example, a filter chamber 7 for filtering the first off-gas, the first off-gas 41 ), such as a THC analyzer (31).

The pretreatment device may further include a filter chamber 7 as well as a knockout drum, which functions to separate the phases of a fluid having two or more phases, a vapor-liquid separator Also called a water separator.

After the first exhaust gas 41 is adsorbed in the concentrator 1, the adsorbed gas 16 coming out of the concentrator 1 is discharged 61 to the atmosphere through the exhaust tower 6 through a conduit. After the adsorption treatment, the gas 16 may pass through an analyzer for the gas 16, such as a THC analyzer 32, before reaching the draw tower 6.

A bypass 12 for the desorbed air 15 entering the concentrator 1 may be formed. The desorbed air 15 is withdrawn through the condenser 1 and mixed with the second exhaust gas 42 to form a gas mixture 8, which is then introduced into the oxidizer 2. The second off-gas 42 is primarily for direct oxidation of volatile organic compounds by the oxidizer 2 .

For example, the intake may be effected by a pressure gradient generated by the air fan 4 for the oxidizer. The desorbed air drawn from the concentrator 1 may pass through an analyzer such as a THC analyzer 33, an LEL analyzer 34, etc. before reaching the oxidizer 2.

The oxidizer 2 is for oxidizing volatile organic compounds included in the mixed gas 8, and preferably, a regenerative thermal oxidizer (RTO) or a direct fired thermal oxidizer is recommended. In addition, a combustible gas (eg, natural gas) 22 for oxidation of volatile organic compounds may be supplied to the oxidizer 2, and pure oxygen or combustion air (for supply of oxygen to the oxidizer 2) 23) may be supplied by a supply means such as a combustion air fan. In the oxidizer 2, the combustible gas 22 is burned by the burner 24, and at this time, volatile organic compounds are also oxidized. Alternatively, the oxidizer 2 may include a heating device for electrically heating the volatile organic compounds contained in the gas mixture 8 instead of the burner 24 .

After combustion treatment in the oxidizer (2), the combustion treatment gas (27) coming out of the oxidizer (2) is discharged (61) to the atmosphere through the discharge tower (6).

As a part of the gas drawn from the oxidizer 2, after the hot air 13 is mixed with the low-temperature temperature control air 14 for forming the desorption temperature, the heat exchanger 11 passes through the desorption heat supply line 5 After supplying heat to the desorption air (15) in ), it is discharged (61) to the atmosphere through the discharge tower (6).

In the concentrating system of the present disclosure, adsorption and desorption processes are performed in a state in which the temperature of the desorbed air 15 and the rotational speed of the rotor of the concentrator 1 are controlled, so that the first exhaust gas 41 and the concentrator 1 , concentrator air fan (3), desorption heat supply (5), discharge tower (6), heat exchanger (11), desorption air bypass (12), hot air (13), temperature control air (14), desorption As described for air 15. When the actuator of the concentrator 1 is a rotor, the rotor may be configured to rotate at 3 to 6 rotations per hour (RPH) by a rotary motor, but is not limited thereto. If the rotational speed of the rotor is too low, the VOC contained in the first exhaust gas 41 is over-adsorbed, exceeding the breakthrough point, and the treatment efficiency in the gas 16 after adsorption treatment may be lowered. Conversely, the rotational speed of the rotor Even when is excessive, the residence time of the fluid in the rotor is reduced, and thus the treatment efficiency in the adsorption or desorption process may be lowered. It should be taken into account that the rotational speed of the rotor affects the proper treatment efficiency or desorption efficiency.

In the concentration system of the present disclosure, air for purging the oxidizer 2 may be supplied through a purging air line 26. The purging air line 26 includes external air (as illustrated by reference numeral 26 in FIG. 2), air after oxidation treatment (27; air after combustion), or air before oxidation treatment (8; mixed gas), depending on the configuration of the process. may be selectively employed, and may be implemented by a method of introducing air into the oxidizer 2 at a positive pressure and a method of removing air from the oxidizer 2 at a negative pressure, depending on the process.

In addition, fresh air may be introduced into the first exhaust gas 41 through a fresh air damper for safety of the process during system operation or in case of emergency, or may be located at the front of the mixed gas 8 to achieve the purpose Depending on this, it may be introduced into the mixed gas (8).

In the concentration system of the present disclosure, monitoring equipment (monitoring system) for managing the mode of concentration and oxidation and controlling the process can be introduced, as illustrated in FIG. 2, a THC analyzer as part of the monitoring system (eg 31, 32, 33), an LEL detector (eg 34), a temperature sensor (exemplified by 'TC' in FIG. 2), a pressure sensor (exemplified by 'PC' in Fig. 2) and a damper (eg, damper actuators 51, 52, 54)/valve control system. Preferably, all monitoring systems having self-monitoring functions, such as redundant equipment, NAMUR NE43 grade equipment, and SIL 2 or higher grade equipment, may be used for safe and stable monitoring.

'VFD' illustrated in FIG. 2 refers to a variable frequency drive, which is mentioned as an example of a drive method that can be used in the system of the present disclosure, so that the drive method of the present disclosure is not limited thereto. This point will be understood by those skilled in the art.

Preferably, electrical control is required in the concentration system of the present disclosure, which can be achieved by an electric MCC (motor control center) panel, a PLC panel, an HMI, and appropriate software. A detailed description thereof is provided in the present invention. are omitted so as not to obscure the gist of

3 is a flowchart exemplarily showing an operation sequence according to a conventional operating method of the volatile organic compound concentration system of the present disclosure.

Referring to FIG. 3, the conventional operation sequence is largely divided into an initial set point (S310), a purging process (S320), a heating (preheating) process (S330), a standby process (S340), a cleaning process (S350), and a shutdown It is divided into processes S360 and S370, but the mode selection process is not included here. In this disclosure, cleaning of the concentrator 1 refers to detachment, and concentrator-RTO cleaning mode refers to continuous detachment of the concentrator 1 and simultaneous operation of the RTO 2 .

4 is a flowchart exemplarily showing an operating sequence according to a switchable operating method of the volatile organic compound concentration system of the present disclosure.

Referring to FIG. 4, the operation sequence according to the operating method of the present disclosure is largely a mode selection process and an initial set point (S410), a purging process (S420), a heating (preheating) process (S430), a standby process (S440), It is divided into a cleaning process (S450) and a shutdown process (S460, S470).

Specifically, at an initial set point (S410), the operation of the oxidizer 2 is started or a batch mode is started according to the selected operation mode.

At the initial set point (S410), if the selected operation mode is the batch mode ('Yes' in S411), the batch mode is started (S414 and S415), and the cleaning process (S450) is performed. At the batch mode selection point (S414), the RTO starting point (S421) or the concentrator cleaning mode (S450) starting point (S452) may be proceeded according to the preparation status of the RTO.

During the purging process (S420), the oxidizer 2 is purged. In the purging process (S420), purging of the oxidizer 2 may be performed for a predetermined time.

During the heating (preheating) process (S430), the oxidizer 2 is heated (preheated). In the heating (preheating) process (S430), the oxidizer 2 is heated over a set temperature and time (S431), and when the set temperature is achieved, the oxidizer 2 performs the standby process (S440). is maintained in

During the standby process (S440), the oxidizer 2 is standby. The standby process (S440) may be maintained (S442) until the transition to the cleaning process (S450) is performed (yes in S441).

In the cleaning process (S450), the volatile organic compounds are removed using the concentrator 1 and the oxidizer 2. In the cleaning process (S450), the desorption air 15 may be heated (S454) according to a set time and temperature.

After the cleaning process (S450), the standby process (S440) may be performed again, and in the standby process (S440), the volatile organic compound is removed by the concentrator 1, and high-temperature desorption (S445) this can be done

During the shutdown processes (S460 and S470), the volatile organic compound concentration system according to the present disclosure is shut down.

In the operation sequence of the present disclosure illustrated in FIG. 4, preparation for operation is completed in a short time, and there is an advantage in that batch type operation of the concentrator is also possible.

Meanwhile, the volatile organic compound enrichment system of the present disclosure requires temperature control for the flow of the desorption air 15, because the temperature of the desorption air 15 must be accurately controlled to prevent concentration runaway. The concentration system of the present disclosure is in batch mode after the complete desorption step through the shutdown process (S460, S470) at the time corresponding to reference numeral 404 in FIG. 1, that is, the production stop / system shutdown period (404). S414, S415), which preferably goes through a high temperature of 200 ~ 220 ℃, preferably takes 60 ~ 120 minutes. Through this operation, the structure including the adsorbent of the concentrator 1 is kept clean and has maximum adsorption capacity.

Next, in the period corresponding to reference numeral 405 in FIG. 1 , that is, the idle or waiting period/batch mode operation period 405 , the system proceeds to the batch mode adsorption step ( S440 ). In its batch mode, the system functions like an activated carbon tower. In this mode (S440), the oxidizer 2 transits to the shutdown mode (S460), in which the desorption processes (S444 and S445) are stopped, and the oxidizer 2 is an oxidizer isolation damper ( 25), the concentrator air fan 3 remains running, and the monitoring system is activated.

After the batch mode, the system may enter the preparation mode during a period corresponding to reference numeral 401 in FIG. 1 , that is, preparation/heating time 401 . From the viewpoint of the present invention, this step can be said to be key and important. In this step, the oxidizer 2 is restarted (S420), and the desorption process starts after moving to the heating process (S430), The temperature rises.

Preferably the temperature should be raised in a time/temperature dependent manner. The solution presented in this disclosure involves temperature control in the manner of two or more steps, preferably the temperature for the desorption air 15 and its holding time is 50°C 30 minutes → 100 ℃ 30 minutes → 150 ℃ 30 minutes → final set point, for example, may be set to 200 ℃, but is not limited thereto.

For example, with respect to this setting, the above 30 minutes can be calculated from the time of the rotation cycle of the disk concentrator 1, preferably, a time of 30 minutes with the time of 2 rotations in the disk concentrator of 4 RPH. this is calculated Similarly, the temperature can be controlled in such a way as to gradually increase the temperature from 50°C to 200°C in 90 minutes.

Activation of the analyzers 31, 32, 33, 34 at the warm-up/heat time 401 and during batch mode operation may cause the system to enter a shutdown mode or a ready-to-use mode. In this case, in order to ensure safety in the system of the present disclosure, emergency bypass means, more specifically, the emergency bypass damper 51 for the first exhaust gas 41 and the emergency bypass damper for the second exhaust gas 42 52, an emergency bypass damper 54 for the mixed gas 8, an emergency rupture disk 53, and the like may be utilized. The safety of the system can be maintained by using self-monitoring or by using redundant, ie redundant sensors and movements.

The rupture disk 53 illustrated in FIG. 2 functions to forcibly release the pressure therein by bursting when the pressure inside the line rises above the set pressure.

In addition, referring to FIG. 5 , it can be seen that fuel consumption is significantly reduced by the system and method of the present disclosure. In addition, it can be seen in FIG. 6 that electricity consumption is also reduced by the system and method of the present disclosure.

7 shows a temperature profile inside the combustion chamber of an oxidizer according to the present disclosure for different days. According to the solution of the present disclosure, it was confirmed that the temperature in the combustion chamber did not runaway and the high temperature alarm was maintained without sounding in the area of the box separately indicated in FIG. 7 . On the other hand, FIG. 8 shows an overview of the temperature inside the combustion chamber when the oxidizer is operated without controlling the desorption temperature/time according to the comparative example. As shown in FIG. 8 , it was confirmed that when the oxidizer was operated without controlling the desorption temperature/time, the temperature inside the combustion chamber of the oxidizer ran out of control, a high temperature alarm sounded, and shutdown occurred.

9 shows a temperature profile inside the combustion chamber of an oxidizer according to the present disclosure for normal operating days. According to the solution of the present disclosure, it was confirmed that the temperature in the combustion chamber did not runaway and the high temperature alarm was maintained without sounding in the area of the box separately indicated in FIG. 9 .

Figure 10 shows a temperature profile following a long-term test inside the combustion chamber of an oxidizer according to the present disclosure. According to the scheme of the present disclosure, it was confirmed that the temperature in the combustion chamber did not runaway and the high temperature alarm remained unaffected.

In short, according to the method and system of the present disclosure as described above, a reliable and safe means for maintaining ventilation is provided for a production process in a discontinuous state, thereby maintaining a low-emission process or operating without fuel consumption. The advantage of being able to maintain the spatial environment, being able to comply with legal emissions, and operating a highly economical air pollution abatement system across multiple technologies, with or without a discontinuous production process, and with or without a separate enrichment plan. there is

Although the present invention has been described above with only a few selected embodiments, those skilled in the art can easily understand the concept on which this disclosure is based, and the concept as a design basis for modified devices for performing some objects of the present invention. will be able to easily use

The foregoing examples are merely illustrative of several possible embodiments of various aspects of the present disclosure, and equivalent modifications may be made by others skilled in the art after reading and understanding this specification and the accompanying drawings. Changes and/or modifications will occur. In addition, even though a particular feature of this disclosure may have been described and/or illustrated with respect to only one of several embodiments, such a feature may be preferred in any given application or in one or more other embodiments of other embodiments that may be advantageous in a particular application. Features can be combined. Also, to the extent that the words "comprising," "includes," "including," "has," "including," or variations thereof are used in the description and/or claims, such terms It is intended to be inclusive in a manner similar to the term "comprising".

1: thickener
2: oxidizer
3: Air fan for concentrator
4: Air fan for oxidizer
5: desorption heat supply
6: discharge tower
7: filter chamber
8: mixed gas
11: heat exchanger
12: Bypass
13: hot air
14: air for temperature control
15: Desorption air
16: gas after adsorption treatment
22: combustible gas
23 Combustion air
24: burner
25: oxidizer isolation damper
26: purging air line
27: gas after combustion treatment
31, 32, 33: THC analyzer
34: LEL analyzer
41: first exhaust gas
42: second exhaust gas
51, 52, 54: emergency bypass damper
53: Rupture Disc
61: final discharge

Claims (30)

In the volatile organic compound concentration system,
A concentrator (1) adsorbing a volatile organic compound contained in a first exhaust gas (41), the concentrator (1) having an adsorption structure including an adsorbent for adsorption treatment of the volatile organic compound, and driving the adsorbent It includes an actuator, a drive, or a flow path change means, and the first exhaust gas 41 is supplied to the condenser 1, and the first exhaust gas 41 is supplied by the adsorbent. a concentrator (1), in which gas (16) after adsorption treatment generated in the adsorption treatment is discharged from the concentrator (1);
a post-adsorption treatment gas conduit connected to the concentrator 1 and discharging the gas after adsorption treatment 16 from the concentrator 1;
An air fan (3) for the concentrator generating a pressure gradient upstream or downstream of the concentrator (1) to transport the gas (16) after adsorption treatment from the concentrator (1) in a direction toward the gas conduit after treatment for adsorption (16). ;
a desorption air supply conduit connected to the concentrator 1 and supplying desorption air 15 for desorbing the volatile organic compound from the adsorbent to the concentrator 1;
a desorption air downstream conduit connected to the concentrator 1 and through which the desorption air 15 discharged from the concentrator 1 passes after the desorption treatment for the adsorbent by the desorption air 15 passes;
Oxidizing a mixed gas (8) in which at least one second exhaust gas (42) containing a volatile organic compound can be further mixed with the desorption air (15) supplied through the conduit downstream of the desorption air at a predetermined joining point. As an oxidizer (2) for processing, the volatile organic compound contained in the mixed gas (8) is reduced by receiving combustion air (23) containing oxygen and a combustible gas (22) and combusting the combustible gas (22). A burner (24) for joint combustion treatment or a heating device for electrically heating the volatile organic compounds of the mixed gas (8), wherein the gas (27) generated in the combustion treatment is transferred to the oxidizer oxidizer (2), exiting (2);
an oxidizer air fan (4) generating a pressure gradient for supplying the mixed gas (8) to the oxidizer (2);
a combustion air fan generating a pressure gradient supplying the combustion air (23) to the oxidizer (2); and
Heat supply means for supplying heat to the desorption air (15)
including,
The volatile organic compound concentration system:
In the first exhaust gas inlet path extending between the first exhaust gas inlet through which the first exhaust gas 41 is introduced and the concentrator 1, the first exhaust gas is formed at a position immediately adjacent to the first exhaust gas inlet. A first emergency bypass damper 51 for forced discharge of (41);
The second exhaust gas 42 formed at a position immediately adjacent to the second exhaust gas inlet in the second exhaust gas inlet path extending between the second exhaust gas inlet through which the second exhaust gas 42 flows and the joining point. ) A second emergency bypass damper 52 for forced discharge of; and
A third emergency bypass damper 54 for forced discharge of the mixed gas 8 formed in the mixed gas supply path extending between the confluence point and the oxidizer 2
Further comprising at least one of, a volatile organic compound enrichment system. According to claim 1,
at a location upstream from the concentrator with respect to the first off-gas, at a location downstream from the concentrator with respect to the first off-gas, and at a location downstream from the concentrator 1 with respect to the desorbed air 15; A volatile organic compound concentration system, wherein analyzers capable of measuring the concentration of pollutants are respectively installed, and operation of the volatile organic compound concentration system according to predetermined operating standards is assisted by the measured values of the analyzers. According to claim 1,
and a bypass (12) for desorption air formed between the desorption air supply conduit and the gas conduit after adsorption treatment. delete According to claim 2,
and a pretreatment device for the first exhaust gas (41) between the inlet of the first exhaust gas (41) and the concentrator (1). According to claim 5,
and a first analyzer (31) for the first off-gas at a location downstream of the pretreatment unit and upstream of the concentrator. According to claim 6,
wherein the first analyzer (31) is a THC analyzer. According to claim 2,
Further comprising a discharge tower 6 for discharging the gas 16 after the adsorption treatment and the gas 27 after the combustion treatment into the atmosphere,
and a second analyzer (32) for the gas after the adsorption treatment between the gas conduit after the adsorption treatment and the discharge tower (6). According to claim 8,
wherein the second analyzer (32) is a THC analyzer. According to claim 1,
and at least one analyzer (33, 34) for the desorbed air (15) in the conduit downstream of the desorbed air or for the mixed gas (8) downstream of the joining point. According to claim 10,
wherein the at least one analyzer comprises at least one of a THC analyzer and a LEL analyzer. According to claim 1,
The heat supply means for supplying heat to the desorption air 15,
a heat exchanger (11) supplying heat to the desorption air (15) upstream of the desorption air supply pipe by using hot air (13), which is part of the gas drawn from the oxidizer (2);
hot air mixing means for mixing hot air (13), which is a part of the gas drawn from the oxidizer (2), with the desorption air (15); and
A desorption heat supplier 5 capable of adding heat to the hot air 13 or directly supplying desorption heat to the desorption air
A volatile organic compound concentration system comprising at least one of According to claim 12,
An air supply conduit for temperature control that controls the temperature of the hot air 13 by supplying air 14 for temperature control to the hot air 13 before the hot air 13 is mixed with the desorption air 15. Further comprising a volatile organic compound concentration system. According to claim 1,
The volatile organic compound concentration system further comprises a purging air line (26) connected to the oxidizer (2) and supplying purging air that is air for purging the oxidizer (2). According to claim 5,
and a first fresh air damper enabling the introduction of fresh air into the first exhaust gas (41) upstream of the pretreatment device. According to claim 15,
The volatile organic compound concentration system of claim 1, wherein the pretreatment device further comprises a filter chamber (7) for filtering the first exhaust gas. According to claim 16,
The volatile organic compound concentration system of claim 1, wherein the pretreatment device comprises a knockout drum. According to claim 1,
and a fresh air damper allowing fresh air to be drawn into the mixed gas (8) upstream of the air fan (4) for the oxidizer. According to claim 1,
The volatile organic compound enrichment system of claim 1 , wherein the adsorption structure has a shape of a polyhedron or a cylinder, and the actuator is provided with means for driving the adsorption structure to change a flow path or changing a flow path passing through the structure. According to claim 1,
wherein the adsorbent is a zeolite. According to claim 1,
wherein the oxidizer (2) is a regenerative oxidizer or a direct fire oxidizer. According to claim 1,
wherein the combustible gas (22) is natural gas or propane gas. A switchable method of operation of the volatile organic compound concentration system of claim 1, comprising:
an initial set point (S410) for starting the operation of the oxidizer 2 or starting a batch mode according to the selected operating mode;
a purging process (S420) of purging the oxidizer 2;
a heating (preheating) step of heating (preheating) the oxidizer 2 (S430);
a stand-by step (S440) of putting the oxidizer 2 on stand-by;
a cleaning process (S450) of removing the volatile organic compounds using the concentrator 1 and the oxidizer 2; and
A shutdown process for shutting down the volatile organic compound concentration system (S460, S470)
A switchable method of operation of a volatile organic compound concentration system comprising: According to claim 23,
At the initial set point (S410),
If the operating mode is the batch mode ('Yes' in S411), the batch mode is started (S414 and S415) and the cleaning process (S450) is performed. According to claim 23,
In the purging process (S420),
A method of switchable operation of a volatile organic compound concentration system in which purging of the oxidizer (2) is carried out for a defined period of time. According to claim 23,
In the heating (preheating) process (S430), the oxidizer (2) is heated over a set temperature and time (S431), and when the set temperature is achieved, the oxidizer (2) is placed in the standby process (S440). A convertible method of operation of a volatile organic compound enrichment system, wherein According to claim 23,
In the standby process (S440),
A switchable operating method of the volatile organic compound concentration system, which is maintained (S442) until switching to the cleaning process (S450) (yes in S441). According to claim 23,
In the cleaning process (S450),
The switchable operating method of the volatile organic compound concentration system, wherein the desorbed air (15) is heated (S454) according to a set time and temperature. According to claim 28,
The heating (S454) of the desorption air 15 is performed over the first temperature, ..., n-th temperature, which is n temperatures that are natural numbers greater than or equal to 2, and the first temperature, ..., n- 1 temperature is maintained for the first holding time corresponding to each of them, ..., the n-1th holding time, or
The heating (S454) of the desorbed air (15) is continuously performed for a predetermined holding time so that the heating temperature is linearly increased with time. According to claim 23,
After the cleaning process (S450), the standby process (S440) is again performed, and in the standby process (S440), the high-temperature desorption (S445) is performed as the volatile organic compound is removed by the concentrator (1) , a switchable method of operation of a volatile organic compound enrichment system.

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