JP5152422B2 - Organic solvent-containing gas treatment system - Google Patents

Description

  The present invention relates to an organic solvent-containing gas treatment system for treating a gas containing a volatile organic solvent, that is, a so-called VOC-containing gas at a low running cost.

  Volatile organic compounds (VOC) such as toluene, isopropyl alcohol (IPA), xylene, methyl ethyl ketone (MEK), and ethyl acetate are used in paint factories, printing factories, and film laminating factories. If it diffuses and floats in the inner space, it will adversely affect the human body. Moreover, if the VOC-containing gas is released into the atmosphere without being treated, the environment will be polluted.

  Therefore, from the viewpoint of preventing air pollution, VOC emission standards are set in regulated plants, and it is obliged to observe the emission standards.

  Examples of gas purification methods for decomposing or removing VOC-containing gas include, for example, a direct combustion method in which VOC-containing gas is directly burned by a burner, a catalytic combustion method in which oxidative decomposition is performed by a catalyst, and a regenerative combustion method in which heat is preheated and burned with a heat storage material However, there is a demand for a processing system that can effectively reduce the processing cost by effectively using the energy generated during combustion, and a VOC-containing gas processing system using a micro gas turbine is practically used for this purpose. It has become.

  FIG. 14 shows a general VOC-containing gas processing system 50 using a micro gas turbine.

  The processing system 50 shown in the figure introduces a low-concentration VOC-containing gas from the raw gas supply pipe 51 into the adsorption region of the concentrator 52, removes VOC by the adsorbent in the concentrator 52, and purifies the purified air. The air is discharged from the air delivery pipe 53 to the atmosphere.

  The concentrating device 52 has a cylindrical shape, and the adsorbent alternately passes through the adsorption region and the desorption region by rotating around the central axis 54.

  In the desorption region, high-temperature desorption air is blown to the adsorbent via the desorption pipe 55, and the VOC adsorbed by the adsorbent is desorbed. At this time, desorption is performed with a smaller air volume than the air supplied from the raw gas supply pipe 51, so that the VOC concentration is increased and sent out from the gas discharge pipe 56.

  The sent VOC-containing gas is sent to the micro gas turbine 57 as a combustion gas, compressed by the compressor 57a, heat exchanged with the exhaust gas discharged from the turbine 57c by the regenerator 57b, and sent to the combustion chamber 57d.

  In the combustion chamber 57d, a mixed gas obtained by mixing combustion gas and fuel is burned, and the turbine 57c is rotated by the combustion gas, and a generator 58 connected to the turbine 57c is driven to generate electric power (for example, patents). Reference 1).

JP 2005-61353 A

  Since the VOC-containing gas discharged from the concentrator 52 is desorbed by high-temperature air, it cannot be sent to the microgas turbine 57 as it is. It is desirable to lower the temperature to be suitable for operation.

  For example, in the case of the micro gas turbine 57 in which the combustion gas temperature is 25 ° C. and a rated output of 285 kW is obtained, when the combustion gas temperature rises to 30 ° C., the 20 kW output decreases, and when it rises to 35 ° C., the 40 kW output decreases, When the temperature is raised to 70 ° C., the required output cannot be obtained.

  Therefore, in the conventional VOC-containing gas processing system using the micro gas turbine 57, the cooling device 59 is indispensable, but the cooling water consumed in a large amount by the cooling device 59 is a factor that increases the running cost. It has become.

  Further, while the amount of combustion gas that can be supplied to the micro gas turbine 57 is limited, there is a large amount of VOC-containing gas that must be generated and processed in the factory. Therefore, there is also a problem that the processing system becomes large in order to reliably process the VOC-containing gas.

  The present invention has been made in view of the problems in the conventional VOC-containing gas processing system, and provides an organic solvent-containing gas processing system capable of processing VOC-containing gas at low running cost and saving energy. It is.

The organic solvent-containing gas treatment system of the present invention rotates a cylindrical adsorbent around its cylinder axis, adsorbs an organic solvent in a gas containing a low-concentration volatile organic solvent to an adsorbent passing through an adsorbing portion, A concentrator that discharges the desorbed gas concentrated by blowing desorption air onto the adsorbent that has adsorbed the organic solvent that passes through the desorption section;
A micro gas turbine having a compressor, a combustor that mixes and burns fuel with the desorption gas compressed by the compressor, and a turbine that is driven by the combustion gas generated by the combustor;
A compressor supply path for supplying a part of the desorption gas to the compressor;
A desorption part return path for returning the remainder of the desorption gas to the upstream side of the desorption part,
The outlet portion of the desorption portion includes a first region partitioned so as to guide the desorption gas having a low temperature to the supply path for the compressor in the rotation direction of the cylindrical adsorbent, and the desorption gas having a high temperature as described above. The gist is that it is divided into a second region partitioned so as to guide the return path for the detachable part.

  In the present invention, the low temperature (or high) means that the temperature is low (or high) as compared to the average desorption outlet temperature in the desorption outlet portion constituted by a single region (not divided).

  In the present invention, a cooling device for cooling the desorption gas can be interposed in the compressor supply path.

  Moreover, the exhaust heat recovery boiler which collect | recovers the heat | fever of the waste gas discharged | emitted from the said micro gas turbine can be provided.

  Moreover, the heat exchanger which heats the desorption air by heat-exchanging the vapor | steam which generate | occur | produced in the said waste heat recovery boiler with the desorption air can be provided.

  ADVANTAGE OF THE INVENTION According to this invention, the organic solvent containing gas processing system which can process VOC containing gas by low running cost and can aim at energy saving can be provided.

It is a principle figure of the concentration apparatus of this invention. (a) is the graph which shows the desorption characteristic of a concentration apparatus, (b) is the table | surface which showed the measured value of the desorption characteristic. It is a perspective view which shows the structure of the disk rotor type | mold concentration apparatus with which this invention is applied. (a) is a perspective view which shows the structure of the cylinder type concentrator to which this invention is applied, (b) is an enlarged view of the desorption outlet part. It is explanatory drawing which shows 1st embodiment of a VOC containing gas processing system. It is explanatory drawing which shows 2nd embodiment of a VOC containing gas processing system. It is explanatory drawing which shows 3rd embodiment of a VOC containing gas processing system. It is explanatory drawing which shows 4th embodiment of a VOC containing gas processing system. (a)-(d) is the graph which showed the relationship between adsorption body rotation speed and desorption performance. It is explanatory drawing which showed the general concentration apparatus corresponding to FIG. It is explanatory drawing which showed the general concentration system corresponding to FIG. It is explanatory drawing which showed the general concentration system corresponding to FIG. It is explanatory drawing which showed the general concentration system corresponding to FIG. It is a block diagram which shows the structure of the conventional VOC containing gas processing system.

Hereinafter, the present invention will be described based on embodiments shown in the drawings.
1. Principle of Concentrator FIG. 1 shows the principle of an organic solvent-containing gas concentrator (hereinafter abbreviated as a concentrator) of the present invention.

  In the figure, a concentrating device 1 for adsorbing an organic solvent in a VOC-containing gas having a large air volume and a low concentration has a cylindrical case 3 that can rotate around a central axis 2. The adsorbent 4 having a honeycomb structure for adsorbing VOC (with the communication path oriented in the central axis direction) is housed to constitute a cylindrical adsorbent as a whole.

  The adsorbent 4 is appropriately selected from activated carbon fiber, zeolite paper, and the like according to the components of the VOC-containing gas.

  An adsorbing portion 1a and a desorbing portion 1b are partitioned on a moving path along which the cylindrical adsorbing body rotates, and an adsorbent (adsorbing body) 4 passes through the adsorbing portion 1a and the desorbing portion 1b alternately. ing.

  In the adsorbing unit 1a, for example, a VOC-containing gas supply pipe 5 for introducing a VOC-containing gas generated in the factory and a purified air for sending purified air purified by the adsorbent 4 of the concentrating device 1 to the factory. A delivery tube 6 is provided.

  Moreover, the desorption part 1b is provided with a desorption air supply pipe 7 for blowing high-temperature dry air, for example, 180 ° C., that is, desorption heating air, onto the adsorbent 4 that has adsorbed VOC. Is set to be about 1/2 to 1/30 of the volume of the VOC-containing gas, so that the desorbed gas is concentrated.

The desorption outlet 1c is provided with a first pipe 8 and a second pipe 9, respectively, in the rotational direction of the cylindrical rotating body, and the first pipe 8 is a processing initial area (first area) in the desorption section 1b. The second conduit 9 is drawn from the late processing region (second region) in the detachable portion 1b.
Next, the purpose of dividing the desorption outlet 1c into a plurality of regions will be described.

2. Characteristics of the concentration device Fig. 2 (a) is a graph showing the desorption inlet temperature, desorption outlet temperature and concentration in the desorption section 1c for the concentration device 1 shown in Fig. 1, and Fig. 2 (b) shows the measurement. Each measured value is shown.

In addition, 2450 ppm CH ₄ of VOC-containing gas (MEK, toluene, MIBK, etc.) was introduced into the adsorption part of the concentrator 1, and 180 ° C. desorption heated air was introduced into the desorption part.

In FIG. 2A, the horizontal axis represents elapsed time (%), the left vertical axis represents temperature (° C.), and the right vertical axis represents gas concentration (ppmCH ₄ ). The elapsed time represents the time from when the cylindrical adsorbent arrives at the start point (zero%) of the desorption part 1b to the end point (100%) of the desorption part 1b. The circumferential suction position at 1b is shown.

  When the desorption heating air is introduced at 180 ° C., the desorption outlet temperature starts to rise with a delay (elapsed time of about 30%), and when the elapsed time reaches 100%, it becomes approximately 180 ° C., similar to the desorption inlet temperature. .

  On the other hand, the concentration of the desorption gas desorbed from the desorption section 1b increases as the desorption outlet temperature rises, and generally peaks at an elapsed time of 50% and then decreases.

  Next, Table 1 shows the measurement results of the air volume, the desorption outlet temperature, and the desorption outlet concentration when the desorption outlet portion 1c is divided into a plurality of regions (first and second regions in this embodiment).

  As can be seen from Table 1, when the area ratio of the desorption outlet 1c is changed and divided into the first and second regions, a desorption gas having a low temperature and low concentration is obtained from the first region of the pattern 1, and the second A desorption gas having a high temperature and a high concentration can be obtained from the region.

  Further, a desorption gas having a low temperature and a relatively high concentration is obtained from the first region of the pattern 2, and a desorption gas having a high temperature and a high concentration is obtained from the second region.

  Furthermore, a desorption gas having a high temperature and a high concentration is obtained from the first region of the pattern 3, and a desorption gas having a high temperature and a relatively high concentration is obtained from the second region.

For comparison, a disk rotor type concentrator 60 (see FIG. 10) is shown as a comparative example. The desorption outlet temperature and concentration are average values, and the air volume is 200 Nm ³ / min.

  In patterns 1 to 3, the low concentration (or high) means that the concentration is low (or high) compared to the average desorption outlet concentration of the desorption portion of the comparative example.

  As described above, if the range from the desorption start point to the desorption end point in the desorption part 1b is divided into the first region and the second region, desorption gases having different characteristics can be selectively obtained.

  The present invention focuses on the fact that desorption gas having different characteristics can be obtained if the desorption outlet 1c is divided into a plurality of parts, and various VOC-containing gas processing apparatuses using desorption gases having different characteristics are embodied.

3. Configuration of Desorption Outlet Portion in Concentrator Next, a specific configuration of the desorption outlet portion 1c will be described for the disk rotor type concentration device shown in FIG. 3 and the cylinder type concentration device shown in FIG.

3-1. Disc rotor type concentrator The disc rotor type concentrator 10 shown in FIG. 3 is configured to rotate a cylindrical adsorbent 11 having a honeycomb structure around a rotating shaft 12, and the VOC-containing gas is cylindrical. Clean air introduced from one of the adsorbents 11 and purified from the other is taken out.

  Ducts 13 and 14 are arranged on both sides of the cylindrical adsorbent 11 so as to face each other. Desorption heated air is blown from the duct 13 to the cylindrical adsorbent 11, and desorption gas is emitted from the other duct 14. It is supposed to be discharged.

  Although the duct 14 faces the duct 13, the outer peripheral side length La of the duct 13> the outer peripheral side length Lb of the duct 14.

  That is, the passage area of the duct 14 is set smaller than the passage area of the duct 13 in the range 14 ′ indicated by the broken line.

  Thus, by changing the ratio of La and Lb, the desorption region can be divided into a desired first region and second region.

  Thereby, the desorption gas C having a relatively low temperature from the first region (compared to the desorption outlet temperature of 90 ° C. in the comparative example) can be led to the first pipe line 8 shown in FIG. The gas D can be led to the second conduit 9.

  In the figure, an arrow A indicates the direction of rotation of the cylindrical adsorbent 11.

3-2. Cylinder type concentrator Fig. 4 shows the configuration of the cylinder type concentrator 20, where Fig. 4 (a) is an external view showing the overall configuration, and Fig. 4 (b) is an enlarged view of the desorption outlet. It is shown.

  The concentrator 20 has a vertical axis V.P. A VOC-containing gas is introduced from the outer peripheral side of the adsorbent 21 toward the center thereof, and the purified clean air is taken out from the space inside the adsorbent 21. .

  With respect to the adsorbent 21 that has adsorbed the VOC, the desorption heated air is blown to the adsorbent 21 from one duct arranged so as to sandwich the adsorbent 21, that is, the desorption air supply pipe 22, and contains VOC. The desorption gas is discharged from the other duct, that is, the desorption outlet 23.

  In FIG. 4 (b), the desorption outlet 23 is branched in a horizontal direction from a duct 23a provided in a vertical direction so as to define a desorption area outlet of the adsorbent 21, and a lower portion of the duct 23a. A first pipe line 23b and a second pipe line 23c are provided.

  In the duct portion 23a, a partition plate 23d is provided in the vertical direction for dividing the desorption region outlet portion into a plurality of regions (two in the embodiment). A shaft 23f projects from the partition plate 23d through a guide groove 23e, and a nut 23g can be fastened to the shaft 23f. Thereby, if the nut 23g is loosened and moved in the left-right direction (arrow B direction), and the nut 23g is tightened at the moved position, the partition plate 23d can be fixed at a desired position, and the outlet portion of the detachment region Can be divided into a first area and a second area at an arbitrary ratio.

  The first region communicates with the first pipeline 23b with the partition plate 23d as a boundary, and the second region communicates with the second pipeline 23c. Thereby, the desorption gas from the desorption region is branched into two pipes 23b and 23c, and is taken out as desorption gas C and desorption gas D.

  The desorption gas C from the first region can be led to the first pipe line 8 shown in FIG. 1, and the desorption gas D can be led to the second pipe line 9 as well.

4. VOC-containing gas treatment system
4-1. First Treatment System FIG. 5 shows a first embodiment of a VOC-containing gas treatment system 30 using the above-described concentrator. In the following description, the same components as those in FIG.

  In addition, the desorption outlet part of the concentration apparatus 1 shown to the same figure is divided | segmented into the 1st area | region shown in the pattern 1 of Table 1, and the 2nd area | region. For convenience of explanation, the desorption gas temperature from the first region is 40 ° C., and the desorption gas temperature from the second region is 130 ° C.

The first region has a lower desorption outlet temperature (90 ° C. → 40 ° C.) and a lower concentration (7,430 → 2,800 ppm CH ₄ ) than the desorption region of the concentrator of the comparative example (single region). Therefore, the VOC-containing gas supply pipe 5 is returned to the VOC-containing gas supply pipe 5 through the first pipe 8 as the adsorption part return path, and is used again as the raw gas, or returned to the detachable air supply pipe 7 and used.

  In the initial stage of desorption, the adsorbent is not sufficiently heated and the desorption concentration is extremely low. Therefore, the desorption gas C having a low desorption efficiency is supplied again to the adsorption process. Moreover, it can adjust so that the flow volume of the desorption gas supplied to the combustion apparatus 31 may not become excessive by it.

On the other hand, the desorption gas D discharged from the second region and having a high temperature (130 ° C.) and a high concentration (10,750 ppm CH ₄ ) is supplied to the combustion device 31 via the second pipe 9 serving as a supply passage for the combustion device. The VOC is oxidatively decomposed.

  Since the desorption gas D is at a higher temperature than the temperature (90 ° C.) of the desorption gas discharged from the concentration device of the comparative example, fuel can be saved.

  As the combustion apparatus 31, a direct combustion apparatus or a catalytic oxidation apparatus can be used.

  The direct combustion device directly contacts the combustible gas with the flame and oxidizes and decomposes it in a high temperature atmosphere of 700 to 850 ° C. for a predetermined time. The catalytic oxidation device preheats the combustible gas to about 200 to 350 ° C. However, they are oxidatively decomposed by passing through a catalyst, both of which are known devices.

  The exhaust gas generated by the combustion of the combustion device 31 is introduced into the heat exchanger 32 and used for heat exchange for heating the desorption air.

When the VOC-containing gas is burned using the concentrator 60 (see FIG. 10) of the comparative example, as shown in FIG. 11, the desorption gas with the average desorption outlet temperature, that is, the desorption outlet temperature (130 of the second region). Since the desorption gas is supplied to the combustion device 61 at a desorption outlet temperature (90 ° C.) lower than (° C.), a fuel saving effect cannot be expected.
In FIG. 11, reference numeral 62 denotes a heat exchanger.

4-2. Second Treatment System FIG. 6 shows a second embodiment of the VOC-containing gas treatment system using the concentrator 1. Note that the same components as those in FIG. 5 are denoted by the same reference numerals and description thereof is omitted.

  6 is also divided into a first region and a second region shown in pattern 3 of Table 1. For convenience of explanation, the desorption gas temperature from the first region is 70 ° C., and the desorption gas temperature from the second region is 160 ° C.

  The processing system 40 burns a gas cooler (cooling device) 33 that cools the desorption gas C discharged from the first region of the concentrator 1, and a mixed gas that is a mixture of the VOC-containing gas cooled by the gas cooler 33 and fuel. And a micro gas turbine 34 that generates power and an exhaust heat recovery boiler 35 that recovers heat of exhaust gas discharged from the micro gas turbine 34.

  Specifically, the desorption gas C is supplied to the gas cooler 33 through the first pipe 8 serving as a compressor supply path, and is lowered to 40 ° C., which is a temperature suitable for the operation of the micro gas turbine 34.

  On the other hand, the desorption gas D is returned to the desorption section upstream side via the second pipe 9 as the desorption section return path.

  As shown in FIG. 12, in a general processing system in which the concentrator 60 and the micro gas turbine 64 are combined, the VOC-containing gas discharged from the concentrator 60 is once cooled by the gas cooler 63 and then the micro gas turbine 64. The exhaust heat recovery boiler 65 recovers the combustion heat generated in the micro gas turbine 64. Since the desorption outlet temperature of the concentrator 60 has risen to approximately 90 ° C., this high temperature desorption gas is removed from the gas cooler. 63 is required to cool to a temperature of 40 ° C. suitable for operation of the micro gas turbine. Therefore, the temperature difference ΔT to be lowered is 50 ° C.

  On the other hand, according to the processing system 40 of the present invention, since the desorption outlet temperature in the first region of the concentrator 1 is 70 ° C., the temperature difference ΔT to be lowered is 30 ° C. That is, a reduction in running cost is expected for a difference of 20 ° C. between the two temperatures.

Specifically, the amount of cooling water saved by the temperature difference is 7 m ³ / h. When converted into money, the running cost is expected to be reduced by about 5 million yen per year. At the same time, the amount of LNG used as a cooling medium to be saved is 4 m ³ / h, and a running cost reduction of 2 million yen per year is expected.

However, when the unit price of cooling water is 70 yen / m ³ , the unit price of LNG is 70 yen / Nm ³ , and the annual operation of the treatment system is 8,000 hours.

4-3. Third Processing System FIG. 7 shows a third embodiment of the VOC-containing gas processing system using the concentrator 1.

  In addition, the desorption outlet part of the concentration apparatus 1 shown to the same figure is also divided | segmented into the 1st area | region shown in the pattern 3 of Table 1, and the 2nd area | region.

  In this processing system 50, similarly to the processing system 40 shown in FIG. 6, a gas cooler 33 that cools the desorption gas C discharged from the first region of the concentrator 1, and the VOC-containing gas and fuel cooled by the gas cooler 33 And a waste gas heat recovery boiler 35 that recovers the heat of the exhaust gas discharged from the micro gas turbine 34.

  The point where the desorption gas C is supplied to the gas cooler 33 through the first pipe 8 as the supply path for the compressor and is lowered to 40 ° C. which is a temperature suitable for the operation of the micro gas turbine 34 is shown in FIG. The desorption gas D is supplied to the combustion device 31 and burned. As a result, the desorption gas C having a relatively low temperature is supplied to the micro gas turbine 34 while reducing the running cost, and the desorption gas D having a high temperature (160 ° C.) is supplied to the second pipeline as the supply path for the combustion apparatus. 9 is supplied to the combustion device 31 through 9 to assist combustion, so that each desorbed gas can be used efficiently.

  The exhaust gas generated in the combustion device 31 is introduced into the heat exchanger 32 and used for heat exchange for heating the desorption air.

  Incidentally, as shown in FIG. 13, in a general processing system in which the concentrating device 60, the micro gas turbine 64, and the combustion device 61 are combined, a part of the 90 ° C. desorption gas is supplied to the micro gas turbine 64. Since the desorption gas that cannot be processed by the micro gas turbine 64 is supplied to the combustion device 61, a loss occurs in the process of cooling the desorption gas to a temperature suitable for the combustion of the micro gas turbine 64. Since the temperature of the desorption gas supplied to the device 61 is too low, a combustion saving effect cannot be expected.

4-4. Fourth Treatment System FIG. 8 shows a fourth embodiment of a VOC-containing gas treatment system in which a plurality of concentrators are arranged.

When the air volume of the VOC-containing gas exceeds, for example, 1000 m ³ , two concentrating devices are arranged, 50% of the VOC-containing gas is used as the adsorption unit of the first concentrating device 1A, and the remaining 50% is used as the second concentrating device 1B. Introduced into the adsorption part.

  However, the first concentrator 1A is a conventional concentrator in which the above-described desorption outlet is divided, and the second concentrator 1B is a conventional concentrator in which the desorption outlet is not divided.

  The desorption heated air is branched and introduced into the desorption portion of the first concentrator 1A and the desorption portion of the second concentrator 1B.

  The desorption gas C1 discharged from the first region at the desorption outlet of the first concentrator 1A is supplied to the gas cooler 33 via the first pipe 8 serving as a compressor supply path, and is suitable for the operation of the micro gas turbine 34. The temperature is lowered to 40 ° C. On the other hand, the desorption gas D1 discharged from the second region is supplied to the combustion device 31 via the second pipe 9 serving as the combustion device supply passage.

  Further, the desorption gas E discharged from the second concentrator 1 </ b> B is merged with the desorption gas D <b> 1 through the merge channel 15 and supplied to the combustion device 31. That is, surplus gas that is discharged from the first and second concentrators 1 </ b> A and 1 </ b> B and cannot be processed by the micro gas turbine 34 is processed by the combustion device 31.

  According to the processing system in which a plurality of the concentrating devices are arranged, VOC can be reliably adsorbed even if the air volume of the VOC-containing gas to be processed is large.

5. Adjustment of Desorption Gas Concentration FIG. 9 shows the relationship between the adsorbent rotational speed and the desorption performance of the concentrator when the desorption inlet temperature is constant.

  As shown in FIGS. 4A to 4D, it can be seen that the desorption outlet temperature, that is, the temperature of the desorption gas increases as the adsorbent rotation speed decreases.

  Further, when the adsorbent rotational speed is 9 rph and 12 rph, the desorption gas concentration is sufficiently lowered in the latter half of the treatment (see the concentration characteristics F1 and F2), that is, the desorption is completed, so that the desorption performance is good.

  On the other hand, if the rotation speed of adsorption is 15 rph or 20 rph, the desorption performance is low since the desorption process is completed before the desorption gas concentration is sufficiently lowered (see concentration characteristics F3 and F4).

  However, as can be seen from FIGS. 4A to 4D, the peak of the desorption gas concentration can be shifted by changing the adsorbent rotational speed. Therefore, if this point is utilized, when the desorption outlet is divided into a plurality of regions, the desorption gas concentration in that region can be controlled.

  For example, when the desorption outlet is divided into a first region and a second region, the peak of the desorption gas concentration is shifted into the first region having a relatively low temperature, or the second region having a relatively high temperature. It is possible to shift the peak of the desorbed gas concentration.

  Therefore, by dividing the desorption outlet into multiple areas and controlling the rotational speed of the adsorbent, the characteristics (temperature, or temperature and concentration) of the desorption gas discharged from each area are arranged in the constructed processing system. It is possible to adjust the elements to be operated (micro gas turbine, combustion device, etc.) so that they can operate efficiently.

DESCRIPTION OF SYMBOLS 1 Concentrator 1a Adsorption part 1b Desorption part 1c Desorption outlet part 2 Center axis 3 Case 4 Adsorbent 5 VOC containing gas supply pipe 6 Purified air delivery pipe 7 Desorption air supply pipe 8 1st pipe (supply line for compressors)
9 Second pipe (return path for desorption)
DESCRIPTION OF SYMBOLS 10 Disc rotor type concentrator 11 Cylindrical adsorber 12 Rotating shaft 13 Duct 14 Duct 20 Cylinder type concentrator 21 Adsorbent 22 Desorption air supply pipe 23 Desorption outlet part 23a Duct part 23b First pipe line 23c Second pipe line 23d Partition plate 23e Guide groove 23f Shaft 23g Nut 30 VOC containing gas processing system 31 Combustion device 32 Heat exchanger 33 Gas cooler 34 Micro gas turbine 35 Waste heat recovery boiler 40 VOC containing gas processing system 60 Concentrator

Claims (4)

Adsorption by rotating the cylindrical adsorber around its cylinder axis, adsorbing the organic solvent in the gas containing low-concentration volatile organic solvent to the adsorbent passing through the adsorbing part, and adsorbing the organic solvent passing through the desorbing part A concentrating device that discharges the desorbed gas concentrated by blowing desorption air on the body;
A micro gas turbine having a compressor, a combustor that mixes and burns fuel with the desorption gas compressed by the compressor, and a turbine that is driven by the combustion gas generated by the combustor;
A compressor supply path for supplying a part of the desorption gas to the compressor;
A desorption part return path for returning the remainder of the desorption gas to the upstream side of the desorption part,
The outlet portion of the desorption portion includes a first region partitioned so as to guide the desorption gas having a low temperature to the supply path for the compressor in the rotation direction of the cylindrical adsorbent, and the desorption gas having a high temperature as described above. An organic solvent-containing gas treatment system, wherein the organic solvent-containing gas treatment system is divided into a second region partitioned so as to be guided to the return path for the desorption part.   The organic solvent-containing gas processing system according to claim 1, wherein a cooling device for cooling the desorption gas is interposed in the supply path for the compressor.   The organic solvent containing gas processing system of Claim 1 or 2 provided with the waste heat recovery boiler which collect | recovers the heat | fever of the waste gas discharged | emitted from the said micro gas turbine.   The organic solvent containing gas processing system of Claim 3 provided with the heat exchanger which heats desorption air by heat-exchanging the vapor | steam which generate | occur | produced in the said waste heat recovery boiler with desorption air.

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