KR100698764B1 - Method for recovery of volatile organic compounds by adsorption-condensation and apparatus therefor - Google Patents

Abstract

A method and an apparatus for recovery of volatic organic compounds by adsorption-condensation are provided to use a moisture removing unit for removing any additional secondary refining process to reuse recovered volatic organic compounds as recovered. An apparatus for recovery of volatic organic compounds by adsorption-condensation includes a moisture removing unit(5A,5B) and an adsorption unit(9A,9B) respectively supplied with air and steam from a heating/cooling unit, so that the moisture removing unit detaches adsorbed moisture indirectly and the adsorption unit detaches adsorbed volatile organic compounds. Moisture-containing air obtained by the detachment of the moisture is discharged to the air and volatile organic compound-containing air obtained by the detachment of the volatile organic compounds is supplied to a condensation unit(19) to be recovered in the liquid phase by a separator(20), wherein unrecovered volatile organic compound-containing air is re-injected into the adsorption unit. The air discharged from the adsorption unit is heated and partially reused in the detachment of the adsorption unit and the regeneration of the moisture removing unit.

Description

Adsorption condensation recovery method and recovery device of volatile organic compounds TECHNICAL FIELD OF RECOVERY OF VOLATILE ORGANIC COMPOUNDS BY ADSORPTION-CONDENSATION AND APPARATUS THEREFOR}

1 is a process flow diagram showing one embodiment of the present invention.

Figure 2 is a flow chart showing a state of producing and transporting the energy required for the regeneration of the water removal device, the desorption of the adsorption device, etc. as the reactor heating / cooling device of the present invention.

3 is a fixed flow chart showing the entire recovery device of the present invention.

Figure 4 is a graph showing the amount of acetone recovery according to the number of operation of the adsorption apparatus according to the present invention.

5 is a graph showing the acetone recovery rate according to the number of operation of the adsorption apparatus according to the present invention.

Figure 6 is a graph showing the water concentration of the moisture removal device outlet according to the operation of the water removal device according to the present invention.

     Explanation of symbols on the main parts of the drawing

     1: Contaminant gas supply direction 2: Blowing pump

     5A, 5B: Water removal device 18: Vacuum pump

     9A, 9B: adsorption device 19: condenser

     37: recovery tank 50: heating / cooling device

The present invention relates to a method for removing and recovering volatile organic compounds generated in the industrial field and an apparatus therefor.

In general, the recovery and removal of volatile organic compounds (VOCs) emitted from industrial sites such as paint shops, refineries, storage stations, storage facilities of various chemical products, printing shops, laundries, drying doctors / dry booths and chemical process units As a method, a combination of combustion, condensation, absorption, adsorption, membrane separation, biofiltration, and more than one process is operated.

In order to recover or remove volatile organic compounds in an industrially useful way, 1) the recovered organic compounds must not contain impurities such as moisture, 2) process cost and equipment cost must be low, and 3) There should be no secondary contamination. And 4) the emission concentration of pollutants contained in the clean gas from which volatile organic compounds have been removed should be managed below the allowable standard value, and 5) the volatile organic compound recovery system should be able to operate in a wide range of low to high concentrations. do.

The combustion process is the simplest among the volatile organic compound removal devices, and can handle pollutant gases at low concentrations. However, in the combustion process, additional auxiliary fuel must be used to treat low concentration of volatile organic compounds, and waste heat generated during combustion is recovered and reused, but it is expensive because it includes expensive solvent loss costs and operation cost of combustion equipment. Phosphorus, of course, generates carbon dioxide, which causes the globally problematic greenhouse effect.In particular, volatile substances include chlorine, nitrogen, sulfur, etc., or in the case of incomplete combustion, secondary pollutants that are fatal to the atmosphere. Creates.

When the condensation process is used for the recovery of volatile organic compounds, it is difficult to recover and remove it when it is not a high concentration of polluting gas, and even if the concentration of the polluting gas is high, the concentration of volatile organic compounds in the gas discharged to the atmosphere after being purified by the condenser It is difficult to manage the concentration below the environmental standard concentration. Cryogenic cooling is required depending on the volatile organic compound, and since the moisture content is high in the volatile organic compound recovered in the condensation process, an additional secondary purification process is required.

The absorption process can be operated in a wide range of low to high concentrations, but the purity of the recovered solvent is not high, and a second purification process is required like a condensation system for recycling, and may cause secondary contamination of the solvent used for absorption. have.

When using membrane separation equipment, the equipment cost is high and the efficiency is low at low concentrations, so it is applicable to the recovery of very expensive volatile organic compounds, but the recovery of general volatile organic compounds and gasoline used as fuels currently used industrially There is economical inadequacy.

However, in the case of the adsorption process, it is possible to operate in a wide concentration range from low concentration to high concentration, the installation cost and operation cost is low, and there is an advantage of simple operation. However, in the case of the existing adsorption process, waste water treatment is required by using desorption and recovery of steam when recovering volatile organic compounds, and in the case of water-soluble volatile organic compounds, there is a disadvantage in that a double treatment is required to separate water from the recovered solvent. have.

In the desorption process using steam, the adsorbent acts as a catalyst by the energy supplied from the steam. Particularly, when the volatile organic compound containing ketones is desorbed, a side reaction is generated by side reaction, and the adsorbent ages. It drastically reduces the amount of adsorption and the adsorbent life.

Therefore, the present invention is a new concept of volatile organic compound recovery device that solves the problems of the existing adsorption process and the above-mentioned condensation process as follows.

a. The introduction of a water removal device in the process solved the problem that an additional secondary purification process was required because it was included in the recovered volatile organic compounds that had been a problem in the existing equipment, and thus the recovered volatile organic compounds could be reused in a recovered state without the secondary purification process. It is possible.

b. By indirectly contacting steam, which is a fluid flowing into the desorption process for recovering volatile organic compounds, without direct contact with the adsorbent, the mixing of volatile organic compounds and water was essentially blocked. Therefore, the recovered volatile organic compounds do not require a secondary purification process, and basically eliminated the possibility of secondary pollutants caused by steam.

c. In the adsorption process, the adsorption efficiency was increased by lowering the temperature of the adsorption device to remove volatile organic compounds that are contaminants more efficiently. Therefore, the pollutant concentration of the emitted clean gas can be managed below the lower allowable concentration, thereby completely solving the air pollution problem.

d. The indirect heating method was used to prevent denaturation (side reaction) due to the high temperature during the desorption of the adsorbed adsorbate, and the manifold adsorption device was introduced to increase the efficiency of the indirect heating. In addition, by introducing an indirect heating method, the desorption temperature can be adjusted according to the desorption heat of various adsorbates.

e. In order to increase the efficiency of the recovery of high concentration volatile organic compounds, it is possible to increase the energy efficiency by installing and operating a cooling condenser at the inlet to stop the operation of the low concentration of volatile organic compounds.

f. In order to make the best use of the adsorption capacity of the adsorption system and to ensure safe operation, it is necessary to estimate the optimum adsorption and desorption transition times. In order to solve this problem, the control method by concentration was used to know the destruction of the adsorption system.

g. The temperature of the water removal device was to adjust the adsorption temperature from room temperature to 150 ℃ in order to prevent the adsorption of volatile organic compounds that are competing with water adsorption.

Accordingly, a first object of the present invention is to provide a method for removing or recovering a volatile organic compound, specifically, air containing a volatile organic compound,

(a) selective adsorption or competitive adsorption removal of moisture from the moisture removal device (5),

(b) condensation apparatus 19 recovers or removes volatile organic compounds by condensing them in a liquid state;

(c) supplying air containing the residual volatile organic compounds to the adsorption device (9) to adsorb and remove the residual volatile organic compounds,

(d) clean air optionally as shown in FIG. 2, heating the temperature range from room temperature to 200 ° C. in the heating / cooling device 50, or a portion of the heated air (0-100%) is removed Supplied to the apparatus 5 to desorb the adsorbed moisture to be discharged to the moisture-containing air, and a portion (0 to 100%) of the heated air is supplied to the adsorption apparatus 9 to absorb the volatile organic compounds adsorbed. The present invention provides a method for recovering a volatile organic compound consisting of desorption and supply to the condenser 19.

In one preferred embodiment of the present invention, as shown in FIG. 2, at least 75% of the heated air exiting the heating / cooling device 50 is directed towards the moisture removal device 5 and 25% of the heated air. The following is adapted to feed toward the adsorption device 9. This distribution ratio (0 to 100%) is realized with a suitable distribution device such as a valve.

In another embodiment of the present invention, the water removal device (5) and the adsorption device (9) is a selected adsorbent such as activated carbon, modified activated carbon, molecular sieve, activated carbon fiber, polymer adsorbent, activated alumina, zeolite series use.

A second object of the present invention is to provide a device for recovering volatile organic compounds, specifically, a water removal device (5) for selectively absorbing and removing moisture from air containing volatile organic compounds, Adsorption device (9) for adsorption and recovery of volatile organic compounds from the air removed in advance, heating / cooling device for cooling the adsorption device to obtain the heated steam for desorption and to increase the adsorption efficiency of the heated adsorption device during desorption 50 is configured as shown in FIG.

In one embodiment of the present invention, the air and steam from the heating / cooling device 50 is supplied to the water removal device 5 to indirectly desorb the adsorbed water, and another portion of the adsorption device ( 9) to desorb the volatile organic compound adsorbed, and the moisture-containing air obtained by desorbing moisture is discharged to the atmosphere, and the volatile organic compound-containing air obtained by desorbing the volatile organic compound is The volatile organic compound-containing air, which is supplied to the condenser 19 and recovered in the liquid phase through the separator 20 and is not recovered, is reintroduced into the adsorption device 9.

In one embodiment of the present invention, the air discharged from the adsorption device 9 is heated to partially desorb the adsorption device, and some (0 to 100%) to be used for regeneration of the water removal device.

In another embodiment of the invention, a mechanical or oil vacuum pump, preferably a mechanical vacuum pump, used for desorption to the adsorption device 9 is connected.

Hereinafter, the configuration of the present invention with reference to the drawings in more detail.

1) Moisture removal device (5A and 5B)

The water removal device is a pretreatment device for removing water in a contaminated gas containing volatile organic compounds.

The structure of the water removal device of the present invention is a structure in which an adsorbent having good chemical or physical bonding strength is filled in a container of an adsorption device such as a tower type or a drum type.

The remover used in the water removing apparatus according to the present invention is generally used as an adsorbent, and it is preferable to use an adsorbent having a polarity on the surface in order to have a good bonding force with water.

Adsorbents that can be used in the present invention include activated carbon, modified activated carbon, molecular sieves, activated carbon fibers, polymer adsorbents, activated alumina, zeolite series, etc. Among them, the most suitable adsorbent is zeolite, activated alumina or silica gel having hydrophilic properties or mixtures thereof. .

The choice of adsorbent is divided according to the substances to be adsorbed and removed. The adsorbent to be filled in the water removal device is selected depending on the volatile organic compounds adsorbed and recovered and physical properties such as molecular size of the water removed in the water removal device or difference in polarity of molecules. The moisture removal adsorption device configured as described above contains an adsorbent having a stronger bonding force with moisture than the general volatile organic compound, and thus can selectively adsorb only moisture by competitive adsorption while preventing adsorption of the volatile organic compound, In general, a volatile organic compound having a high molecular weight cannot be adsorbed by using an adsorbent having a constant distribution, and thus a device for removing moisture by causing selective adsorption to allow adsorption to only water having a relatively small molecular size. The pore size and distribution of the adsorbent used are determined by the type of volatile organic compound adsorbed.

By adsorbing and removing the water in this way, it is possible to recover only pure volatile organic compounds having little or no moisture in the condensation step and the adsorption step, which are the recovery steps of the volatile organic compounds.

The desorption process of transferring the adsorbed moisture from the adsorbent back into the air is substantially an adsorbent regeneration process and allows for continuous operation of the device.

The clean air heated in the heating / cooling device is in direct contact with the adsorbent of the water removal device, and the heated steam flows to the outer wall of the water removal device to increase the temperature of the adsorbent in the water removal device, thereby using the dried air and steam heated with moisture. Moisture adsorbed on the adsorbent is desorbed back into the air.

The purified gas introduced to the water removal device is a dry and clean gas with or without water and volatile organic substances removed. Therefore, the indirect heating method is used to increase the temperature to remove the water from the water removal device. Desorption can be advanced by. Such a water removal device is in a state in which water is stored as an adsorbent or the like and is discharged to the atmosphere together with a purified gas from which volatile organic compounds are removed, and a discharge device thereof is known in the art.

2) Adsorption device 9A and 9B

The adsorption device can be tower or drum type or any other type.

The adsorbents used in the adsorption apparatus are used to remove volatile organic compounds, and those whose surface is nonpolar are preferable. Adsorbents for the adsorption device that can be used in the present invention may refer to activated carbon, modified activated carbon, molecular sieve, activated carbon fiber, polymer adsorbent, zeolite series, and the like, which are widely used in the industry.

The most suitable adsorbents used in the apparatus of the present invention are modified activated carbons, zeolite series, polymer adsorbents. The modified activated carbon adsorbent is superior to existing activated carbon and other adsorbents in terms of binding capacity as well as volatile organic compounds. In addition, since the heat of adsorption is small, side reactions of volatile organic compounds hardly occur at the surface of the adsorbent when the volatile organic compounds are adsorbed and then desorbed for regeneration. Therefore, the recovered volatile organic compounds have little or no side reaction products. Therefore, in the case of using such an adsorbent, the object of the present invention that can recover the volatile organic compounds with better purity than the volatile organic compounds recovered by the conventional adsorption-desorption process using activated carbon can be more easily achieved. In addition, the modified activated carbon solves problems such as lack of firmness of existing activated carbon, secondary contamination by dust, secondary reaction of volatile organic compounds containing ketones, and small adsorption amount due to low specific surface area of zeolite. It can be adsorbent.

The purpose of the organic compound adsorption device (9) is to remove the volatile organic compounds from the gas containing the volatile organic compounds of low concentration, concentrate and store them in the adsorption device, and then adsorb the saturated adsorption of a small amount of hot cleaning gas when saturated. It is introduced into the device to produce a gas containing a high concentration of supersaturated volatile organic compounds.

3) Condenser (19)

The condenser 19 is a device for directly recovering volatile organic compounds by rapidly lowering the temperature of air containing high temperature and high concentration of supersaturated volatile organic compounds to a very low temperature. The second purpose is that the unrecovered volatile organic compounds are re-introduced into the adsorption devices (9A, 9B) and mixed with the volatile organic compounds that have passed through the water removal device to lower the temperature of the gas, thereby improving the efficiency of the endothermic reaction. It is in the height.

4) Heating / Cooling Units (50)

In order to remove volatile organic compounds adsorbed and stored in the adsorption device 9 from the adsorption device 9 by desorption and recover the volatile organic compounds in the condenser 19 more efficiently, It must be supersaturated. It is used to increase the temperature of the cleaning gas and the adsorbent flowing into the adsorbed adsorption device to make such a supersaturated state of high temperature, and indirectly heats the dry gas and the adsorbent from which the volatile organic compounds are removed from the adsorption devices 9A and 9B. It is a device for desorbing water adsorbed to the removal devices 5A and 5B.

5) Vacuum Pump (18)

In order to remove volatile organic compounds adsorbed and stored in the adsorption system from the adsorption system by desorption and to recover volatile organic compounds in the condenser more efficiently, the volatile organic compounds should be in a supersaturated state at high temperature during desorption. In order to make such a high temperature supersaturated state, desorption should proceed while minimizing the flow rate of the cleaning gas flowing into the adsorbed adsorption device. Therefore, since the cleaning is not simply the purpose of the desorption, the adsorption device should not be introduced into the adsorption gas under pressure by a blower or the like, and the desorption should proceed under reduced pressure by a vacuum pump or the like. Suitable vacuum pumps used in this case should be mechanical, not oil. For this reason, when an oil type vacuum pump is used, a part of the oil in the pump is evaporated and mixed with the cleaning gas, which remains as impurities in the recovered volatile organic compounds.

Hereinafter, with reference to Figure 1 will be described the operation method and conditions of the method and apparatus of the present invention.

First of all, the numbers in the square of the pipe connected to the water removal device and the adsorption device of FIG. 1 are 1 (absorption WA1) -2 (deal WA1) -3 (deal WB1) -4 (deal WB1). -5 (absorption WB2) -6 (deal WA2) -7 (deal WB2) -8 (absorption WB2) -9 (absorption VA1) -10 (deal VA1) -11 (deal VB1) -12 (deal VB1) -13 (Absorption BA2) -14 (talorol VA2) -15 (talortal VB2) -16 (absorption VB2).

Looking at the action made in each of the above in more detail, the process is made as follows.

The contaminated gas flowing through line 1 is a mixed gas containing volatile organic compounds and moisture in the atmosphere. This mixed gas is introduced into the water removal device 5A or the water removal device 5B through the line 3 and the line 4A or the line 4B to remove water by the principle of selective adsorption and competitive adsorption. And then to line 7 via line 6A or line 6B.

At this time, the water concentration of the discharged gas is from 0g / ㎥ to 10g / ㎥. At this time, the most suitable concentration of water is from 0g / ㎥ to 0.5g / ㎥. At this time, the moisture concentration discharged to the line 7 is a reference for controlling the valve (4A, 4B, 6A, 6B, 31A, 31B, 32A, 32B). Therefore, the moisture removal device 5A and 5B are made of a cycle of adsorption and desorption.

The gas mixed with the volatile organic compounds from which water has been removed is introduced into the adsorption device 9A or the adsorption device 9B through the line 7. The gas introduced into the adsorption device 9A or 9B selectively adsorbs only volatile organic compounds and the pure dry air is discharged through the lines 10A, 10B and 11. At this time, the emitted gas is operated at 0 ~ 0.5g / ㎥, and it is appropriate to manage the emission concentration below the environmental standard emission allowance or allowable concentration.

This discharge concentration serves as a reference for controlling the valves 8A and 8B, the valves 10A and 10B, the valves 15A and 15B and the valves 16A and 16B. The polluted gas which flowed in by the line 7 by these valve control advances adsorption-desorption cycle in 9A of adsorption apparatus or 9B.

The gas discharged from the line 11 after being treated in the adsorption device 9A or the adsorption device 9B is a clean gas from which volatile organic compounds and water are removed. The flow rate of the gas used as the cleaning gas in the clean gas is determined between 0 and 100% of the cleaning gas by the type and concentration of the volatile organic compounds adsorbed by the adsorption device 9A or 9B. However, in general, the flow rate of the cleaning gas among the clean gas discharged from the line 11 is 0.1% to 25%, the most suitable ratio is 1.0% to 15% is most advantageous for operating the device.

The clean gas discharged from the line 24 is heated by the heating / cooling device 50 of FIG. 2 to the line 24, the line 29 and the line 31A or the line 31B at 0-100% of the flow rate. Desorbs and removes the adsorbed water introduced into the water removal device 5A or the water removal device 5B through and then contains only water through the line 32A or the line 32B and the lines 33 and 35. Gas is released into the atmosphere.

And the remaining flow rate of 0-100% or less is introduced into the adsorption device (9A, 9B) through the line 12 and the line (15A, 15B).

The temperature range preheated in the heating / cooling device 50 of FIG. 2 is determined according to the type of volatile organic compound, and the general temperature range is operated at 150 ° C. at room temperature. However, after the cleaning gas flows into the adsorption device 9A or the adsorption device 9B, a temperature having high cleaning efficiency or desorption efficiency should be selected without causing side reactions in the desorption process, and the most advantageous temperature range is 50 ° C to 120 ° C. ℃.

Thus, the cleaning gas is preheated and introduced into the adsorption device 9A or the adsorption device 9B through the line 12, the line 15A or the line 15B, and the volatile organic compounds adsorbed by the high temperature and pressure desorption are removed. A gas containing supersaturated volatile organic compounds is produced and introduced into the vacuum pump 18 through the line 16A or the line 16B and the line 17 and then introduced into the condenser 19 so that the volatile organic compound is introduced. It is recovered.

At this time, the recovered volatile organic compounds are stored in the recovery tank through the trap 20 and the line 37, and the gas containing some of the volatile organic compounds is combined with the line 7 through the line 23 and then the adsorption device ( 9A) or flows into the adsorption device 9B and is reprocessed.

As a further role of the heating / cooling device 50 of FIGS. 2 and 3, there is a cooling function of the adsorption device 9A or the adsorption device 9B. After desorption of saturated adsorption adsorber with depressurization and high temperature cleaning gas, when the volatile organic compound is introduced into the adsorption device, the temperature of the adsorption device is initially high. Therefore, normal adsorption does not occur until the temperature drops by the incoming gas. Therefore, in order to prevent this, the desorption process is carried out by a high temperature cleaning gas to the saturated adsorption device 9A or the adsorption device 9B, and then coolant flows to the outer wall of the adsorption device 9A or the adsorption device 9B. It serves to increase the adsorption efficiency by lowering the temperature of the adsorption device during the cycle.

2 and 3, the operating relationship of the heating / cooling device 50 of the present invention is briefly shown. In the water removing device, 17 (with cold WA) -18 (with cold WB) -19 (with WA) Out) -20 (SUB WB) -21 (Cold WA B) -22 (Cool WB) -23 (SWA) -24 (SBB) -25 (Cold WA) 27 (with cold VA) -28 (with cold VB) -29 (with SVA out) -30 (with SB out) -31 (with cold VA out) -32 (with cold VB out) -33 (with SVA) -34 (With VA) -35 (cold cup VA) -36 (cold cup VB).

The methods and apparatus according to the invention can be modified in a manner that does not depart from the spirit and spirit of the invention, all such variations or modifications being included within the scope of the invention.

In addition, experiments for recovering acetone as a water-soluble solvent using the adsorption condensation type recovery method and recovery device for volatile organic compounds of the present invention were performed as follows.

As shown in the graphs shown in Figs. 4, 5 and 6, Figs. 3 to 5 show the acetone recovery amount, the recovery rate and the amount of water contained in the acetone at the outlet of the water removal device according to the operation of the adsorption device and the water removal device. Figure is a graph.

The switching time of the A and B devices of the adsorption device and the water removal device was set to 60 minutes. To separate the water, the water tower was filled with an acetone called ADZ500 and a water separation adsorbent that can selectively separate water. The VOCs tower was filled with an ADC70C adsorbent for acetone adsorption and recovery. The temperature of the water removal device was maintained at 20 ~ 70 ℃ (selectively adjusted according to the solvent to be recovered). In the case of adsorption equipment, the adsorption process was maintained by keeping the reactor at 15-25 ℃ to increase the adsorption efficiency. In the case of desorption, side reactions of the VOCs recovered in the range of 100 to 155 ° C. did not occur. For this purpose, the heating / cooling device 50 used a steam boiler. The total injected flow rate was 3500 L / min and the injection amount of acetone was 80 g / min in the liquid phase. The liquid acetone was vaporized while passing through a hot pump and introduced into the reactor. The total amount of acetone injected at one time conversion was about 4.8 kg. The humidity in the air was 9-12 g / m ³ . The VOCs reactor was subjected to continuous experiments by switching reactors A and B. The water tower was operated by switching reactors A and B at the conversion time.

Figure 4 shows the recovery of acetone according to the conversion number of the adsorption device. As can be seen from the graph, the amount of acetone added was continually recovered, almost similar to 4.8 kg. The recovery rate also showed a high recovery rate of 90-100%. Water removal rate of the water removal device also showed a low concentration of less than 1.0% as shown in FIG.

As shown in the above experimental example, it can be seen that the effect is increased by the heating / cooling apparatus of the present invention.

According to the adsorption condensation type recovery method and recovery apparatus of the volatile organic compounds of the present invention, there is an effect that can prevent the loss of resources as well as environmental conservation.

Since the volatile organic compounds recovered from the existing volatile organic compound recovery apparatus contains a large amount of impurities such as water, the recovered volatile organic compounds have to be purified or used as secondary volatile organic compounds. And the process cost of the recovery device is required a lot or the adsorption efficiency is low. In addition, in order to manage the concentration of volatile organic compounds contained in the air discharged to the atmosphere after purification to a much lower level than the environmental standard, a lot of process costs are required. However, the novel apparatus of the present invention has the feature of reusing the recovered volatile organic compounds without the need for an additional purification process with higher efficiency and lower process operating costs than the existing volatile organic compound recovery apparatus.

Claims (8)

Air containing volatile organic compounds, (a) adsorptive removal of water by selective or competitive selection using a heating / cooling device in the water removal device (5), (b) introducing air containing volatile organic compounds from which moisture has been removed to the adsorption device (9) to adsorb pure volatile organic compounds in the adsorption device (9), and adsorbing volatile organic compounds to steam from the heating / cooling device. Or indirectly desorbed using cooling water and recovered in a liquid state through the condenser 19, (c) supplying air containing uncondensed residual volatile organic compounds to the adsorption device (9) to adsorb and remove the residual volatile organic compounds, (d) A part of the clean air is supplied to the moisture removing device 5 to desorb the adsorbed water and is discharged to the water-containing air, and a part of the clean air is supplied to the adsorption device 9 for adsorption. Adsorption condensation type recovery method for volatile organic compounds, characterized in that the volatile organic compounds are desorbed and supplied to the condensation device (19). 2. The adsorption condensation of volatile organic compounds according to claim 1, wherein the clean air from the adsorption device (9) is supplied to the 0-100% moisture removal device (5) and the rest is supplied to the adsorption device (9). Formula recovery method. The method of claim 1 or 2, wherein the water removal device (5) and the adsorption device (9) use an adsorbent selected from activated carbon, modified activated carbon, zeolite, molecular sieve, activated carbon fiber, polymer adsorbent. Adsorption condensation recovery method of organic compounds. The method of claim 1 or 2, wherein the heating / cooling device heats the outer circumferential surfaces of the adsorption device (9) and the water removal device (5). Water removal device (5) for selectively adsorption and removal of moisture from the air containing volatile organic compounds, adsorption removal of pure volatile organic compounds by flowing air containing the water-removed volatile organic compounds directly from the water removal device (5) Heating / cooling device for indirect desorption using high temperature steam or cooling water with adsorption device (9), adsorption device (9) and moisture removal device (5) to adsorb volatile organic compounds, and recovery of volatile organic compounds into liquid phase It is provided with a condenser device 19, Mixing the gas containing some of the volatile organic compounds that are not condensed in the condenser 19 and flowing through the line 23 together with the gas that has passed through the water removal device 5 to supply the adsorption device 9 again. Adsorption condensation type recovery apparatus for volatile organic compounds. 6. The method of claim 5, wherein the water removal device (7) and the adsorption device (9) are each provided with two or more, each of which is supplied with adsorption air is continuously supplied to the other while providing desorption heating air to one of them. Adsorption condensation type recovery apparatus for volatile organic solvents. 7. The method of claim 5 or 6, wherein the air discharged from the adsorption device (9) is brought into contact with steam and cooling water generated in the heating / cooling device to regenerate the water removal device (5), to desorb and heat the adsorption device (9). Adsorption condensation type recovery apparatus for volatile organic compounds, characterized in that to be supplied to the cooling of the adsorption device (9). 7. The adsorption condensation type recovery apparatus for volatile organic compounds according to claim 5 or 6, wherein a mechanical or oil vacuum pump used for desorption is connected to the adsorption device (9).

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