KR200225298Y1 - Treatment system for Volatile Organic Compounds - Google Patents

Abstract

The present invention relates to a VOC treatment system, which has a boiling point higher than that of VOC to be absorbed and is an affinity and repeated organic solvent that absorbs most of the VOC and then repurifies and reuses it at a boiling point difference. The poor amount (less than 1%) of VOCs can be removed or incinerated with activated carbon to provide a safe and economical high efficiency VOC treatment system that can significantly reduce the replacement cycle (replacement cost) and incineration fuel costs of activated carbon. .

Description

Treatment System for Volatile Organic Compounds

The present invention relates to a VOC (Volatile Organic Compounds) processing system, which is a volatile organic solvent, and specifically, absorbs almost all of VOCs having a lower boiling point as an organic solvent having higher affinity and higher boiling point while having affinity with VOC to be absorbed. After recovery, it can be purified and reused at the difference in boiling point, and the amount of VOC that is not absorbed (less than 1%) is adsorbed and removed or incinerated with activated carbon, which greatly reduces the replacement cycle of activated carbon and greatly reduces the replacement cost. The savings and incineration fuel costs have been significantly reduced to provide an efficient and safe VOC treatment system.

VOC (Volatile Organic Compounds), which is a generic term for hydrocarbon compounds and represented by volatile organic compounds, affects the atmosphere in various forms. In particular, it is not only a cause of photochemical smog such as ozone, but also a harmful substance such as carcinogenicity, a cause of global warming and destruction of the stratospheric ozone layer, and an odorous substance in the atmosphere.

In addition, as the research reports that it is also involved in the damage of crops and forests caused by acid rain, it is attracting attention as a global environmental problem, and the treatment methods and means have been steadily studied with a lot of hard work.

VOC emission sources are classified into artificial and natural sources. Natural sources are also known to contribute significantly to VOC emissions, but due to lack of data, only artificial sources are usually considered for management.

VOC emissions have increased significantly due to the rapid increase in the use of gasoline fueled vehicles and the expansion of the use of oils and organic solvents, and the use of other solvents such as painting facilities, emulsification facilities and adhesives, rather than mobile sources such as automobiles, Emissions from fixed sources, such as metal surface treatment facilities, are much higher.

Thinners used as paint organic solvents are evaporated and volatilized into the atmosphere during the film formation process. Therefore, hydrocarbons and gasoline vapors in automobile exhaust gas, chlorine organic solvents for cleaning, gasoline, thinner, benzene, toluene ( C ₆ H ₅ CH _3, boiling point: 110.6 ° C.).

Sources of anthropogenic VOCs are very diverse in type and size, and unlike general pollutants such as SO _X and NO _X , there are difficulties in facility management due to the fact that the outlets are scattered like unspecified emissions such as leakage. The main sources of anthropogenic VOCs that have been known so far are known as the manufacture / use of oil solvents and automobile emissions, although VOCs are released from various sources and react with active substances present in the atmosphere. The representative substance is OH Radical, which VOC reacts with

RH + OH → H ₂ O + R

R + 0 ₂ → RO ₂

Alkylperoxy Radical (RO ₂ ) is produced during the reaction. It reacts with nitrogen monoxide (NO) to generate RO and NO ₂ . Subsequently, in the reaction of RCH ₂ 0 + 0 ₂ → RCHO + HO ₂ , one of the hydrogen atoms of the alkyl proxy radical RCH ₂ 0 is lost, and a hydrohydroxy radical (HO ₂ ) is formed. HO ₂ reacts with NO to become OH Radical and NO ₂ .

As such, NO reacts rapidly with ozone (O ₃ ) in the absence of RO ₂ and HO ₂ radicals, resulting in NO ₂ and O ₂ . However, the presence of radicals above creates a path through which these radicals react with NO, making ozone difficult to decompose. Atomic oxygen (O) produced by NO ₂ photolysis reacts with oxygen molecules (O ₂ ) to generate ozone (O ₃ ), which is difficult to decompose in the presence of radicals such as HO ₂ and RO ₂ . Increases.

In this process, VOC contains oxygen molecules and becomes an alkyl proxy radical, and when photochemical reaction occurs, it becomes a harmful oxygen-containing hydrocarbon such as formaldehyde and PAN (Peroxy Acetyl Nitrate: CH ₃ COO ₂ NO ₂ ). .

In the presence of VOC, nitrogen oxides, and sulfide oxides, photochemical reactions occur to form nitrates, sulfates, and suspended particulate matter. These products fall to the ground and are contained in dry deposits and raindrops. This affects the ecosystem of plants, soils, etc. As such, since VOC is one cause of photochemical air pollution, it is necessary to suppress the emission as much as possible.

Currently, various volatile organic solvents (VOCs), which are environmental pollutants generated in production facilities using organic solvents such as coating facilities and textile coating facilities, are currently adsorbed by activated carbon adsorption towers or rely on incineration.

The activated carbon adsorption facility has a problem that it takes a lot of trouble to have to replace the activated carbon to the limit of the adsorption capacity and processing cost due to the replacement of activated carbon.

The incineration VOC treatment facility has a problem in that the incineration of the VOC treatment facility is not economical because a large amount of exhaust gas and fuel or electricity required to warm the VOC to the incineration temperature are excessively consumed.

Accordingly, the present invention aims to absorb almost all VOCs by using an organic solvent which has a boiling point higher than VOCs to be absorbed, which has affinity and stability with VOCs, and can be used repeatedly.

In addition, an organic solvent absorbing VOC is heated to below the boiling point of the VOC, so that the VOC having a low boiling point can be separated and purified and reused.

In addition, a low amount (less than 1%) of VOCs that cannot be absorbed by adsorption with activated carbon can be removed or incinerated, thereby significantly reducing the replacement cycle of activated carbon, thereby significantly reducing replacement costs and incineration fuel costs. The purpose is to provide.

In addition, two organic solvent tanks that absorb VOCs are configured in a set to continuously operate the VOCs and to continuously purify and recover the absorbed VOCs at boiling points.

In order to achieve the above object, the absorption tower absorbs most of the VOC with an organic solvent having affinity for VOC and having a higher boiling point than VOC, and absorbs a small amount of VOC that is not absorbed with the organic solvent. It is largely composed of a refining apparatus for refining and liquefying by boiling point difference, a recuperation apparatus for circulating and recovering an organic solvent for repeated use, a heat exchanger, and a combustion apparatus for burning and treating unrecovered VOCs.

The characteristics of the present invention is that by developing an organic solvent that can repeatedly recover VOC, it can be used continuously and purified, thereby reducing the cost of organic solvent, and having high boiling point and high viscosity and odorless organic solvent, low boiling point VOC (volatile Organic solvent) is absorbed and treated. Organic solvents used for VOC absorption should be liquid organic solvents such as thermal oils or heavy oils with high boiling point and high viscosity, odorless, chemically stable and VOC absorbed (affinity).

In addition, the solvent tanks are installed in pairs to alternately operate for absorption of VOCs and purification of the absorbed VOCs, and as the organic solvent temperature rises in the solvent tanks, the VOC absorption capacity decreases. Use to lower the temperature of the organic solvent to the appropriate temperature (10 ℃ ~ 30 ℃).

In addition, two (1) sets of (organic) solvent tanks are operated alternately so that VOC absorption and purification can be continued without stopping.

The recovered VOC in the present invention can be purified and reused, the organic solvent can be recovered and used repeatedly, and less than 1% of the unrecovered VOC is adsorbed or burned to activate carbon. The incineration of VOCs is extremely low, so the fuel used for combustion is insignificant. Therefore, it is possible to solve the conventional problems at a low cost operating environment of the industry using the VOC.

1 is a block diagram of the present invention.

2 and 3: VOC (volatile organic solvent) absorption process configuration of the present invention.

4: VOC (volatile organic solvent) purification process configuration of the present invention.

<Explanation of symbols for main parts of the drawings>

(VOC)-Organic Solvent (AS)-Adsorption Tank

(B1) (B2)-Fill (BF)-Blowing Fan

(CB)-Activated Carbon (CS)-Condenser

(CT)-cooling tower (CV1)-(CV5)-check valve

(D)-Demister (DT)-Space

(FB)-Flashback Arrestor (HD)-Trapper

(DW)-Exhaust Pipe (FB)-Secondary Burner

(FD)-Year (FF)-Incinerator

(HE)-Heat Exchanger (M1) (M2)-Manometer

(MF)-Micro Filters (MIX)-Agitator

(P1) (P2)-injection pump (P3)-solvent pump

(P4)-Recovery pump (P5) (P6)-Cooling pump

(PS)-Pressure gauge (PP)-VOC origin

(SC)-Absorption Tower (SN1) (SN2)-Nozzle

(SR)-Suction Tank (ST)-Outlet

(T1) (T2)-Solvent Tank (T3)-Recovery Tank

(T4)-cooling tank (T5)-evaporation tank

(TF)-Turbofan (TM)-Thermometer

(V1-V27)-Valve (WS)-Water Supply

Hereinafter, described in detail with reference to the accompanying drawings a preferred embodiment of the present invention as follows.

The VOC treatment system of the present invention has an affinity with VOC and a boiling point higher than that of VOC, and it is an organic solvent that absorbs most of the VOC and absorbs a small amount of VOC that is not absorbed by activated carbon. To purify and liquefy the liquid to the boiling point difference from the organic solvent, liquefy to recover and circulate and recover the organic solvent repeatedly, a heat exchanger for the absorption and purification of VOC, and a small amount of evaporated VOC. It is largely composed of a combustion device.

1 is a configuration diagram of a VOC treatment system of the present invention, and various VOCs discharged from a VOC generation point PP such as various production facilities or manufacturing facilities include a collector HD and a turbo fan such as a hood or a duct. TF) to the absorption tower (SC) is absorbed / adsorbed.

Most collectors (HD) installed in the VOC generation point (PP) is installed in a structure that can effectively collect various organic solvents (VOC) that volatilizes up. For example, the upper part is narrow and the lower part is a funnel-shaped collector, which is connected to the turbo fan (TF) and the absorption tank (SR) through a connector.

The absorption tower (SC) is composed of an absorption tank (SR) located in the lower portion and the adsorption tank (AS) located in the upper portion, one side of the absorption tank (SR) absorbs the VOC of the VOC generation point (PP) Turbo fan (TF) to be introduced into the lower portion of the SR is connected, the discharge port (ST) through which the clean air from which the VOC is removed is discharged is installed in the upper portion of the adsorption tank (AS).

A plurality of fillers B1 and B2 are installed in multiple layers at intervals in the absorption tank SR installed below the absorption tower SC, and the solvent tank T1 is disposed above the fillers B1 and B2. Alternatively, a plurality of nozzles SN1 and SN2 are respectively provided for injecting the organic solvent supplied from T2 into the fillings B1 and B2.

The VOC supplied to the absorber SR rises while exiting between the fillings B1 and B2, and is mostly absorbed by the organic solvent injected downward. Since the VOC and the organic solvent are organic solvents having affinity for each other, the VOC and the organic solvent are easily mixed / absorbed, and since the boiling point of each other is different, the VOC and the organic solvent are easily separated during purification.

Since the temperature of the VOC flowing into the absorption tank (SR) is maintained at 70 ℃ ~ 80 ℃, so that the organic solvent temperature of the solvent tank (T1) (T2) rises VOC absorption capacity is lowered, such as heat exchanger (HE) Using a cooling means of the same type to lower the temperature of the organic solvent and VOC to an appropriate temperature (10 ℃ ~ 30 ℃).

A discharge pipe DW is installed at the lower end of the absorption tank SR to discharge the organic solvent absorbing most of the VOC while falling from the nozzles SN1 and SN2, and the connection pipe and the valve V3 are provided at the discharge pipe DW. A pair of solvent tanks (T1) and (T2) connected to (V4) are connected so that the absorption of VOC using the organic solvent and the purification operation of separating the VOC absorbed from the organic solvent and the organic solvent can be continued. .

That is, while one side of the solvent tank (T1) is connected to the absorption tower (SC) by opening and closing the valve to absorb the VOC with the organic solvent while the solvent tank (T2) of the other side that has already absorbed the VOC in Figure 3 or 4 It is connected to the purification device of the configuration such as to separate the VOC and the organic solvent by the difference in boiling point, and after the absorption of the VOC and the purification process of the absorbed VOC is completed by operating the valve to change the role of the solvent tank (T1) (T2) Since the absorption of the VOC and the purification of the absorbed VOC are carried out, the absorption and purification of the VOC can be continued alternately, thus improving productivity.

The organic solvents contained in the solvent tanks (T1) (T2) are organic solvents having high viscosity, no volatility and odor, affinity with VOCs, boiling points higher than VOCs, and chemically stable organic solvents such as heavy oil or fruit oil. In order to accommodate the solvent, the organic solvent absorbs the VOC, so that the volume is slightly expanded to secure a space (volume) that can sufficiently accommodate the expansion of the VOC.

Since boiling points of gasoline, thinner, benzene, toluene (C ₆ H ₅ CH ₃ ), and cycillin, which are representatives of VOC, are within 100 ° C and outside (the boiling point of toluene is 110.6 ° C), the boiling point of organic solvent The heat medium oil of 300 ℃ ~ 500 ℃, which is 2-5 times higher than the boiling point of VOC, is used. Therefore, when the VOC is purified, it is easy to separate / purify VOC with low boiling point and VOC with high boiling point. The VOC can be recovered, and the organic solvent separated from the VOC can be repeatedly used to absorb the VOC by recovering it into a solvent tank using a solvent pump (P3).

The solvent tanks T1 and T2 may of course vary in volume depending on the VOC throughput (absorption).

One end of the solvent tanks T1 and T2 is connected to an inlet of the injection pumps P1 and P2 through a connecting pipe having valves V7 and V8 and another valve V11 and V18. Between the outlet of the pumps P1 and P2 and the heat exchanger HE, the valves V12 and V13 and the check valve CV1 and CV2 are respectively connected by a connecting pipe and connected through the heat exchanger HE. The pipe is connected to the nozzles SN1 and SN2 via valves V1 and V2 to form a VOC absorption line.

The solvent tanks T1 and T2 are VOCs according to the opening / closing states of the valves V3, V4, V7, V8, V11 and V12 and the driving states of the injection pumps P1 and P2. It can be operated alternately for absorption or purification of absorbed VOCs.

That is, the valves V3, V7, V11, and V12 are opened, and the valves V4 and V9 are closed. When the injection pump P1 is driven, the organic solvent of the solvent tank T1 is injected into the injection pump P1. VOC absorption line (absorption path) flowing from heat exchanger (HE) → nozzle (SN1) (SN2) → filler (B1) (B2) → discharge pipe (DW) → solvent tank (T1).

In addition, the valves V4, V7, V18, and V13 are opened, and the valves V3 and V10 are closed. When the injection pump P2 is driven, the organic solvent of the solvent tank T2 is injected into the injection pump P2. ), Another VOC absorption line (absorption path) flows from the heat exchanger (HE) → nozzle (SN1) (SN2) → filler (B1) (B2) → discharge pipe (DW) → solvent tank (T2). Alternately, when these processes are operated alternately, VOC absorption and VOC purification can be performed simultaneously.

On the other hand, the adsorption tank (AS) installed on the upper portion of the absorption tower (SC) is composed of the demister (D) and activated carbon (CB), the trace amount (B1) (B2) and the trace amount that was not absorbed by the organic solvent ( Less than 1%) of VOC and the evaporating traces of organic solvent are removed by adsorption.

That is, the activated carbon (CB) installed on the upper portion of the absorption tank (SR) is composed of the activated carbon and the mesh to prevent the separation of the activated carbon is stored, the shape can be formed in a cylindrical or square cylinder shape or polygonal cylinder shape. have.

Although not shown in the drawings, upper and lower portions of activated carbon (CB) are provided with a door for removing activated carbon at the end of its life and a door for inserting new activated carbon, respectively.

A discharge port ST for discharging clean air is installed in the space portion and the upper portion formed inside the activated carbon CB, and the space portion DT is formed around the activated carbon CB, and activated carbon CB is formed. Outside of the plurality of demisters (D) are installed at appropriate intervals.

The demister (D) spatially connects the absorption tank (SR) and the adsorption tank (AS) separated up and down, and the air flowing into the absorption tank (SR) through the demister (D) Ascend to (DT) and then guide activated carbon (CB) to exit the outlet (ST). The demister (D) is a plurality of layers of mesh (網 目) to remove most of the particulate solvent.

That is, a small amount of VOC and organic solvent which are not absorbed in the absorption tank SR and rises along the discharge air are contacted (collisions) with the demister D and are condensed into oil of coarse particles by condensation. As a result of falling to the absorption tank (SR), a small amount of VOC and organic solvent rising along the exhaust air are removed.

The trace amount of VOC and organic solvent which could not be removed even in the demister (D) rises to the space portion (DT) together with the discharge air, passes through the activated carbon (CB), and is mostly adsorbed and removed from the activated carbon (CB) and into the outlet (ST). Clean air is exhausted.

On the other hand, a manometer for measuring and detecting the pressure difference between the joining chamber (inner space of the activated carbon) and the lower part of the demister (D) in which the air discharged from the activated carbon (CB) joins. Manometer (M1) is installed, it is possible to determine the exchange time of activated carbon (CB) due to the pressure difference measured / detected by the manometer (M1) it is possible to replace the activated carbon (CB) at the appropriate time .

Since most of the VOC is absorbed by the organic solvent and the demister (D), the service life of the activated carbon (CB) is greatly increased, and the cost of replacing the activated carbon can be greatly reduced.

That is, in the case of a conventional VOC treatment system without an absorption facility, since most VOCs are adsorbed and treated with activated carbon, the lifetime and replacement cycle of the activated carbon was very short, which required a lot of maintenance costs, but the present invention did not absorb the organic solvent. Since only VOC less than% is adsorbed and removed by activated carbon, the life and replacement cycle of activated carbon is greatly increased and maintenance cost can be drastically reduced.

In addition, the upper and lower portions of the fillings B1 and B2 are provided with another manometer meter M2 that measures and detects the pressure difference between the fillings B1 and B2. Since the exchange time of B1) and B2 can be determined, the fillings B1 and B2 can be replaced at an appropriate time.

In the above, the detection unit for detecting the pressure difference of the manometer (M1) (N2) and the comparison circuit for comparing the pressure difference and the alarm circuit are installed, but the appropriate standard for exchanging activated carbon (CB) and the filling (B1) (B2) The pressure difference inputted from the pressure (set pressure) and the manometer (M1) (N2) is judged to exceed the reference pressure or more than the reference pressure, the alarm may be activated to automatically alarm in such a case it will be very convenient.

On the other hand, since the temperature of the VOC flowing into the absorption tank (SR) is maintained at 70 ℃ ~ 80 ℃, the temperature of the organic solvent of the solvent tank (T1) (T2) rises VOC absorption capacity is lowered, such as heat exchanger (HE) Using a cooling means of the same type to lower the temperature of the organic solvent and VOC to an appropriate temperature (10 ℃ ~ 30 ℃).

That is, by installing the temperature sensor (TM) in the discharge pipe of the turbo fan (TF) to measure and display the temperature of the VOC supplied to the absorption tank (SR), a plurality of installed on the top of the filling (B1) (B2) The nozzle SN is connected to the heat exchanger HE by a connection pipe having valves V1 and V2, and the heat exchanger HE and the cooling tower CT are connected by a connection pipe having a valve V24. Between the HE and the cooling tank T4, a connecting pipe having a valve V22, a cooling pump P5, a valve V21 and a check valve CV4 are sequentially connected, and at one side of the cooling tank T4. The valve V23, the water supply pipe, and the water supply source WS are connected to supply the cooling water, and a cooling water circulation path is formed between the heat exchanger HE, the cooling tower CT, and the cooling tank T4.

Therefore, the organic solvent whose temperature is raised by absorbing the VOC of 70 ° C. to 80 ° C. is cooled to 10 ° C. to 30 ° C. while passing through the heat exchanger HE, and the heat exchanger HE absorbs the heat of the organic solvent. The cooling water flows into the cooling tower CT, is cooled to the ambient temperature (space temperature), and then supplied to the cooling tank T4. The cooling water of the cooling tank T4 is forced to the heat exchanger HE by the cooling pump P5. Supplied. Therefore, the organic solvent supplied to the nozzles SN1 and SN2 is continuously cooled.

One end of the cooling tower CT is connected to the condenser CS with a connection pipe having a valve V25, and between the cooling tank T4 and the condenser CS, the valve V26, the cooling pump P6, and the valve V27. ) And the check valve (CV5) are connected to the connecting tube in order to purify the absorbed VOC to form a cooling line (cooling furnace) for condensing to a low temperature of 10 ℃ ~ 30 ℃ much lower than the boiling point of the VOC.

One end of the solvent tank (T1) (T2) is connected to the inlet of the solvent pump (P3) through the valve (V9), V10, (V14), the outlet of the solvent pump (P3) and the solvent tank (T1) (T2) ) Is connected to the valve (V15) and the check valve (CV3) to prevent backflow of the solvent, the micro filter (MF) to filter impurities or particulate impurities in the returned organic solvent and another valve (V5) (V6) The upper part of the evaporation tank T5 is connected to the connection pipe between the check valve CV3 and the valve V6 through another valve V16, and the inlet port of the solvent pump P3 and the evaporation tank ( The lower part of T5 is connected to a connecting pipe having a valve V17 to form a recovery line (return) for recovering the organic solvent in the solvent tank absorbing VOC to the evaporation tank T5.

On the other hand, when one solvent tank absorbing VOC is saturated or absorbs VOC above a certain level, the solvent is transferred to an evaporation tank (T5) to undergo an evaporation process that is a previous step for purification.

That is, when one side of the solvent tank (T1) absorbs the VOC and becomes saturated, the other side of the solvent tank (T2) forms an absorption line to alternate the duties to absorb the VOC, the valve (V9) (V14) located in the recovery line When (V17) (V15) and (V16) are opened and the solvent pump P3 is operated, the organic solvent in the solvent tank T1 absorbing VOC is transferred to the evaporation tank T5.

When the organic solvent absorbing the VOC is completely transferred to the evaporation tank T5, the boiling point of the VOC is lower than the boiling point of the VOC by a heating means such as an electric heat heater or incinerator FF installed under the evaporation tank T5. The organic solvent is heated to a temperature, for example 40 ° C. to 80 ° C.

In the above, the VOC is volatilized even at the natural temperature, but the VOC absorbed by the organic solvent by heating is separated from the organic solvent more rapidly and evaporates (evaporates), so that the evaporation time (purification and recovery time) can be greatly shortened. , The rising VOC gas is collected into the recovery tank T3 as the liquid flows into the condenser CS through which the cooling water circulates through the chamber CB, and the liquid VOC collected in the recovery tank T3 is the recovery pump P4. It can be recycled (reused) after being filtered out.

Since the heating temperature of the organic solvent is heated to 40 ° C. to 80 ° C., which is below the boiling point of VOC, the heating temperature does not reach 3 to 5 times higher than the boiling point of the much higher organic solvent, thereby preventing volatilization or evaporation of the organic solvent. Easily separated / purified

In the present invention, the upper portion of the solvent tank (T1) (T2), the recovery tank (T3) and the evaporation tank (T5) is connected to the chamber (CB) by a connecting pipe, and blown between the chamber (CB) and the condenser (CS) By installing the fan BF, a small amount of VOC gas evaporating and rising inside these tanks T1, T2, T3, and T5 is collected in the chamber CB and then flows into the condenser CS where the coolant is circulated. It is liquefied / purified and recovered to the recovery tank T3.

Even if the organic solvent of the evaporation tank (T5) is heated above, the evaporation effect is lowered because the VOC evaporates only on the upper surface of the organic solvent. Therefore, in the present invention, by installing a stirring device (MIX) before and after the 60 RPM on the upper part of the evaporation tank (T5) to agitate the heated organic solvent with the stirrer (MIX) so that the VOC can evaporate very effectively and quickly.

In addition, in the present invention by installing an oil gauge or a water gauge in each tank (T1) (T2) (T3) (T4) (T5) to be able to check the liquid level of the aqueous solution, respectively.

On the other hand, when the evaporation of the VOC is completed, only the reduced organic solvent remains in the evaporation tank T5, and the valves V9, V14, and V16 are closed and the other valves V17, V15, and V5 are opened. Next, when the solvent pump P3 is driven, the organic solvent from which the VOC is separated and removed is returned to the solvent tank T1, so that the solvent pump P3 can be repeatedly used to absorb the VOC. In this process, the organic solvent can be repeatedly used, thereby reducing the maintenance cost of the organic solvent.

In addition, the condenser (CS) is forced to circulate the cooling water to effectively liquefy by cooling the VOC evaporated from the evaporation tank (T5) and each tank (T1) (T2) (T3), the appropriate temperature (10 ℃ ~ 30 ℃) Keep it.

The condenser CS is the cooling water supplied to the cooling tank T4 by the open valves V25, V26, V27 and cooling pump P6, the cooling pump P6, the cooling tower CT and the cooling tank ( Since a water cooling line is formed between T4) and the condenser CS, the temperature of the condenser CS is maintained at a temperature of 10 ° C. to 30 ° C. suitable for liquefying the VOC, so that the gaseous VOC is liquefied by the condenser CS. Recovered to tank T3.

Cooling water passing through the condenser (CS) in the above is the temperature is increased by the thermal reaction, but is cooled to 10 ℃ ~ 30 ℃ while passing through the cooling tower (CT) flows into the cooling tank (T4) and is also circulated along the cooling line The check valve CV5 prevents the back flow of the coolant.

The cooling tank T4 is supplied with the cooling water by the water supply source WS connected to the upper part, and the cooling water of a certain level is always supplied / maintained by the level control means such as the rich man.

3 and 4 illustrate an absorption line for absorbing VOC using a solvent, and FIG. 4 illustrates the recovery of VOC absorbed by the organic solvent to a temperature below the boiling point, separated / purified from the organic solvent, and then liquefied. The purification line is shown.

At the rear end of the condenser CS, a combustion device for burning and treating a small amount of VOC gas that has not been condensed (liquefied) is connected.

That is, a flashback arrestor (FB) for preventing the back flow of the flame generated by the combustion of the VOC gas at the rear end of the condenser (CS), and an incinerator (FF) for incinerating the VOC gas is connected to the connection pipe, the flashback arrestor ( FB) prevents explosion due to backflow of flame, overheating of connection pipe and rapid corrosion of connection pipe, and burner (FB) and flue (FD) are respectively installed in incinerator (FF) and condensed in condenser (CS) If not, a small amount (about 1%) of VOC exhaust gas is warmed up to 70 ℃ ~ 80 ℃ and completely incinerated before being discharged to the atmosphere.

The burner (FB) can be incinerated VOC while using fossil fuel or operating an electric heater periodically or as needed. The burner (FB) has a small amount of discharged VOC and can be incinerated sufficiently with an incinerator (FF) to burn it. Fuel costs for warming or incineration are significantly reduced compared to the prior art.

Although not shown in the present invention as a whole, a pressure gauge (PS) is connected to a connection pipe or a tank to which pressure is applied or acted so that the pressure can be checked at any time, and a safety valve is installed at a relatively high pressure, and the temperature is checked. Install the thermometer (TM) on each of these necessary parts.

In addition, in the present invention, it is possible to fully automate these processes by using an electronic open / close valve instead of each open / close valve and a control device having a control circuit, a control program, and a driver circuit for driving the actuator.

The present invention described above is not limited to the above-described embodiments and the accompanying drawings, and various substitutions, modifications, and changes are possible within the scope without departing from the technical spirit of the present invention, which is a technical field to which the present invention belongs. It is self-evident for those of ordinary skill in Esau.

As described above, the present invention has an effect of absorbing almost all of the VOC by using an organic solvent having a higher boiling point than the VOC to be absorbed and repeatedly used.

In addition, the present invention is heated to a temperature below the boiling point of the VOC is absorbed by the VOC absorbed organic solvent has a high boiling point and low boiling point of the VOC can be separated and purified by the difference in boiling point is recovered.

In addition, the present invention is to reduce the replacement cycle of activated carbon by significantly reducing the replacement cycle of activated carbon by removing or incinerated VOC less than 1% (trace) VOC that is not absorbed by organic solvents, and also fuel and fuel for incineration It is effective to provide a low cost and high efficiency VOC treatment system that can greatly reduce the cost.

In addition, the present invention has the effect that the continuous absorption of the VOC and the absorbed VOC can be continuously purified and recovered by the difference in boiling point while operating two alternating organic solvent tanks that absorb VOC in a set.

In addition, the present invention is an organic solvent that absorbs VOC has affinity with VOC, high viscosity and boiling point, odorless, chemically stable liquid such as heavy oil or heat medium oil using the organic solvent to ensure safety and reliability When the VOC is separated / purified, it can be recovered and reused as a solvent tank while filtering with a micro filter, thereby reducing the maintenance cost.

In addition, the present invention can be recycled by refining and recycling the VOC recovered by organic solvent, and clean air is discharged by treatment of adsorption removal and incineration by activated carbon, so that the environmental problem of the industry can be treated at low cost. It is possible to solve the problems in the prior art, such as the effect is very useful design.

Claims (12)

In a system for adsorbing VOC with activated carbon, an organic solvent having a high viscosity, odorless affinity with VOC and higher boiling point than VOC, a solvent tank in which the organic solvent is stored, and an organic solvent circulated through the VOC absorption line Water-cooled cooling system, pump for circulating organic solvent to absorption line, and organic solvent and filler injected into nozzle to absorb most of VOC flowing from VOC generation source, but small amount of VOC which is not absorbed is absorbed by activated carbon Volatile organic solvent treatment system composed of absorption tower. According to claim 1, wherein the VOC absorbed organic solvent is heated to below the boiling point of the VOC, the purification apparatus for separating and liquefying the VOC by the difference in boiling point, and a recovery apparatus for recovering the repeated use of the organic solvent purified VOC separated; And a heat exchange device for liquefying the purified VOC, and a combustion device for combusting a small amount of VOC to evaporate. According to claim 1 or claim 2, Absorption tower (SC) consisting of the absorption tank (SR) and the adsorption tank (AS) is connected to the turbo fan (TF) for supplying VOC to one side of the absorption tank (SR) And a plurality of nozzles SN1 (SN2) for spraying the organic solvent, which is cooled and supplied from the solvent tank, into the fillings B1 and B2 in the absorption tank SR in which the plurality of fillings B1 and B2 are installed. The adsorption tank (AS) is composed of the demister (D) and activated carbon (CB) to adsorb and remove a small amount (less than 1%) of VOC that is not absorbed by the filler (B1) (B2) and the organic solvent, Volatile organic solvent treatment system by installing outlet (ST) through which VOC is removed clean air. The solvent tank of the other side according to claim 1 or 2, wherein one side of the solvent tank T1 is connected to the absorption tower SC to open and close the valve to absorb the VOC with the organic solvent. T2) is connected to the purification device having a heating means to separate and purify the VOC and the organic solvent by the difference in boiling point, and after the absorption of the VOC and the purification process of the absorbed VOC is completed, by operating the valve to the solvent tank (T1) (T2) Volatile organic solvent processing system, characterized in that by changing the role of the VOC absorption and purification of the absorbed VOC to enable continuous shift operation. The injection pump (P1) according to claim 1 or 2, through a connecting pipe having valves (V7) and V8 at one end of the solvent tanks (T1) and (T2) and another valve (V11) and (V18). Connect the inlet of P2), connect the valves V12 (V13) and check valve CV1 (CV2) with the connection pipe between the outlets of the injection pumps (P1) (P2) and the heat exchanger (HE), The connecting pipe passing through the group (HE) is connected to the nozzle (SN1) (SN2) via the valve (V1) (V2) to form a VOC absorption line, characterized in that the volatile organic solvent treatment system. The manometer according to claim 1 or 2, further comprising a manometer measuring a pressure difference between the confluence chamber and the lower end of the demister D in the confluence chamber through which the air discharged from the activated carbon CB joins and the lower part of the demister D. M1) is installed to determine the exchange time of activated carbon (CB) volatile organic solvent treatment system, characterized in that. The method according to claim 1 or 2, wherein a manometer meter M2 for detecting a pressure difference is provided at the upper and lower portions of the fillings B1 and B2 to determine the replacement timing of the fillings B1 and B2. A volatile organic solvent treatment system characterized by the above. According to claim 1 or 2, The plurality of nozzles (SN) installed on the top of the filling (B1) (B2) is connected to the heat exchanger (HE) by a connection pipe having a valve (V1) (V2), The heat exchanger HE and the cooling tower CT are connected by a connection pipe having a valve V24, and the connection pipe and cooling pump P5 having a valve V22 between the heat exchanger HE and the cooling tank T4. And a valve (V21) and a check valve (CV4) in turn, and forming a cooling water circulation path between the heat exchanger (HE), the cooling tower (CT) and the cooling tank (T4). The valve V26 according to claim 1 or 2, wherein the condenser CS is connected to a connection tube having a valve V25 at one end of the cooling tower CT, and the valve V26 is connected between the cooling tank T4 and the condenser CS. And a cooling pump (P6), a valve (V27) and a check valve (CV5) are connected in sequence to form a cooling line for condensing and liquefying the absorbed VOC. The inlet of the solvent pump P3 is connected to one end of the solvent tanks T1 and T2 through the valves V9, V10 and V14. The outlet and the solvent tank (T1) (T2) are connected to the valve (V15) and the check valve (CV3), the micro filter (MF), another valve (V5) (V6) and the connection pipe to prevent the backflow of the solvent, The connection pipe between the check valve CV3 and the valve V6 is connected to the upper portion of the evaporation tank T5 through another valve V16, and the inlet of the solvent pump P3 and the lower portion of the evaporation tank T5 are connected to each other. Volatile organic solvent processing system, characterized in that for connecting the connection pipe having a valve (V17) to transfer the organic solvent of the solvent tank absorbing VOC to the evaporation tank (T5) to form a recovery line for evaporation. The volatile organic solvent treatment system according to claim 1 or 2, wherein a stirring device (MIX) before and after 60 RPM is provided in the upper portion of the evaporation tank (T5). The flame arrester (FB) and the incinerator (FF) for preventing the backflow of the VOC gas flame are provided at the rear end of the condenser (CS), and the burner (FB) is installed in the incinerator (FF). And a flue (FD), respectively, to incinerate a small amount (less than 1%) of VOC exhaust gas that cannot be evaporated and condensed.