KR100802987B1 - Recovery equipment of solvent from styrofoam liquid waste - Google Patents

Abstract

An evaporation system is provided to recover a solvent easily and improve recovery ratio of the solvent within a short time as compared with an existing batch type evaporation tank by evaporating a waste styrofoam slurry dissolved by a solvent, thereby recovering the solvent. As a solvent recovery equipment comprising a slurry storage tank, an evaporator(11), a heat exchanger and a recovery tank, a recovery equipment of a solvent from a waste styrofoam slurry is characterized in that the evaporator comprises: a first cylinder(14) and a second cylinder(15) which have different diameters and are integrally formed at upper and lower sides; a slurry inlet(16) and a gas outlet(17) formed on an upper portion of the first cylinder; a residue outlet(18) formed on the bottom of the second cylinder; a spring type reactant guide(19) which is disposed concentrically within the second cylinder and extends longitudinally to increase retention time of a reactant; and a conical slurry guide(20) which is formed on a boundary part between the first and second cylinders, and which has a plurality of holes formed along the circumference of the guide so that a predetermined amount of slurry can stay in the holes, and the holes are spaced from one another in an equal distance, wherein the slurry can flow down uniformly as a whole along an inner wall surface of the second cylinder while the slurry is discharged downward through the plural holes.

Description

Recovery equipment of solvent from styrofoam liquid waste

1 is a schematic view showing the overall configuration of a solvent recovery apparatus according to the present invention

2 is a cross-sectional view showing an evaporator in a solvent recovery apparatus according to the present invention.

3 is a graph showing the correlation between the temperature and the recovery rate in the recovery process of the solvent from the waste styrofoam slurry using the solvent recovery apparatus according to the present invention

<Explanation of symbols for the main parts of the drawings>

10: slurry storage tank 11: evaporator

12 heat exchanger 13 recovery tank

14: primary cylinder 15: secondary cylinder

16 slurry inlet 17 gas outlet

18: residue outlet 19: reactant guide

20: slurry guide 21: nitrogen gas injector

22: confirmation window 23: diffusion cone

24: valve 25: residue reservoir

The present invention relates to an apparatus for recovering a solvent from a waste styrofoam slurry, and more particularly, to recovering a solvent from a waste styrofoam slurry in which waste styrofoam discharged in large quantities from a fish farm, a waste disposal plant, a farm and fish market, a building site, an electronic shopping mall, and the like are melted in a solvent. The present invention relates to a solvent recovery apparatus capable of economically recovering a solvent used in application by implementing an evaporation system that can easily and increase the recovery rate of solvent in a short time.

In general, a system for reducing waste styrofoam and recycling the waste styrofoam is mainly used by melting the waste styrofoam into heat and compressing it into an ingot, or by using frictional heat by high-speed rotation.

However, in the case of waste rich in aquaculture farms, the treatment method by heat treatment should remove shellfish, seaweed, and tied strings attached to the waste rich, and small sand particles such as shells buried in the waste rich after There is a problem in that the physical properties of the recycled polystyrene is greatly reduced by acting as a foreign matter to the polystyrene.

In addition, it is necessary to remove the moisture contained in the lungs and perform the work, such work requires a lot of manpower has a disadvantage that takes a long time and labor costs.

In addition, there is a disadvantage in that the additional cost of fuel and power consumption is consumed when the waste rich.

In addition, a large amount of harmful gases are generated in the conventional application process by melting the waste rich to generate another environmental problem, and in particular, the existing method is difficult to develop because of the use of power is essential.

Therefore, in order to solve the problem of the system for melting and reducing the existing waste rich, a solvent method of recovering polystyrene by melting the waste rich with a solvent and then evaporating the solvent has been developed.

However, the present solvent system is disadvantageous in terms of economics such as a long time to completely recover the solvent in the process of recovering the solvent, low solvent recovery rate.

Accordingly, the present invention provides a new evaporation system that can easily recover the solvent and increase the recovery rate of the solvent in a short time as compared with the conventional batch evaporation tank by recovering the solvent from the waste styrofoam slurry melted by the solvent. There is a purpose.

The present invention for achieving the above object is a slurry reservoir for supplying the waste styrofoam slurry melted in the solvent, an evaporator for the reaction of the waste styrofoam slurry, a heat exchanger for the liquefaction of the evaporated gas, a recovery tank for the recovery of the solvent Is a solvent recovery device comprising, the evaporator having a different diameter and integrally formed in the upper and lower cylinders, the slurry inlet and gas outlet formed on the upper portion of the primary cylinder, Residual outlet formed in the lower portion of the secondary cylinder, and arranged in the concentric circle in the interior of the secondary cylinder is extended along the longitudinal direction is configured to include a reactant guide in the form of a spring to increase the residence time of the reactants It is characterized by.

In addition, the reactant guide for the retention of the reactant is characterized in that it is installed in the center of the secondary cylinder.

In addition, the boundary between the primary cylinder and the secondary cylinder is characterized in that the slurry guide in the form of a cone having a hole for the retention and input of the slurry is provided.

In addition, the secondary cylinder is characterized in that it further comprises a nitrogen gas injector for helping the discharge of the gas generated by the reaction.

In addition, the slurry inlet of the primary cylinder is characterized in that the confirmation window for observing the inflow of the waste styrofoam slurry melted by the solvent is provided.

Hereinafter, an embodiment of the solvent recovery apparatus according to the present invention with reference to the accompanying drawings in detail as follows.

1 is a schematic view showing the overall configuration of a solvent recovery apparatus according to the present invention, Figure 2 is a cross-sectional view showing an evaporator in the solvent recovery apparatus according to the present invention.

1 and 2, the apparatus for recovering the solvent from the waste styrofoam slurry melted by the solvent is a slurry reservoir 10 for slurry supply, an evaporator 11 for reaction, heat exchange for liquefaction of gas Group 12, a recovery tank 13 for recovery of the solvent, and the like.

Accordingly, the waste styrofoam slurry in the storage tank 10 is introduced into the evaporator 11, and the gas generated in the evaporator 11 is liquefied through the heat exchanger 12 to the recovery tank 13 for solvent recovery. Is collected.

In more detail, the waste styrofoam slurry in which the waste styrofoam is melted in a solvent is stored in the slurry storage tank 10.

In this case, any solvent can be used as long as it can melt waste styrofoam. Specifically, a conventional organic solvent such as toluene, benzene, styrene, ethylbenzene, methylene chloride, isopropyl alcohol, or dilaimonene A natural vegetable solvent may be used, and more preferably, a solvent having a boiling point lower than 240 to 280 ° C., which is a reaction temperature of the secondary cylinder, is used.

In addition, the concentration of the waste styrofoam slurry is approximately 20 to 50% by weight. If the slurry concentration is less than 20% by weight, there is no economic efficiency according to the logistics cost. There is a problem that is not easy.

The waste styrofoam slurry melted in the solvent is continuously injected into the primary cylinder 14 of the evaporator 11 through the slurry reservoir 10.

At this time, the temperature of the primary cylinder 14 is a heat exchanger through the primary cylinder 14 after the gas generated by the reaction in the secondary cylinder 15 moves to the upper layer of the evaporator 11 by nitrogen gas injection It is preferable to maintain a suitable temperature range for reaching above the boiling point of the solvent when discharged to the (12) side, more specifically 150 to 200 ℃.

At this time, if the temperature of the primary cylinder 14 is less than the boiling point of the solvent, the evaporation gas is hardly generated. If the temperature is maintained above 200 ° C., the solvent is evaporated suddenly like a dolby phenomenon. The range was limited to 150-200 degreeC.

In addition, the rate of injecting the waste styrofoam slurry from the slurry reservoir 10 into the evaporator 11 is suitably set to 5 ~ 8 ml / min, which is a solvent when the injection rate of the slurry is less than 5 ml / min Immediately evaporates and hardening of polystyrene, which is a solid, occurs at the inlet of the evaporator. Therefore, it is difficult to inject the raw materials smoothly. If it exceeds 8 ml / min, the solvent evaporates rapidly, which makes it difficult to control the operation. Limited to 8 ml / min.

Next, the slurry injected into the primary cylinder 14 of the evaporator 11 is introduced into the secondary cylinder 15 which is heated to a constant temperature to react.

The evaporator 11 has a cylindrical shape of a double tube, and a slurry inlet port 16 through which the slurry is introduced, and a gas outlet port 17 through which the toluene gas generated by the reaction is evaporated and discharged are formed. In the lower portion, a residue discharge port 18 through which the remaining polystyrene can be discharged is formed.

For example, the evaporator 11 is composed of a large diameter primary cylinder 14 and a small diameter secondary cylinder 15 made of a form in which pipes of different diameters are integrally connected up and down. The boundary portion between the primary cylinder 14 and the secondary cylinder 15 is provided with a slurry guide 20 formed along the inner circumferential wall to form a predetermined volume with the wall, and is introduced through the slurry inlet 16. The slurry may remain in the slurry guide 20 in a predetermined amount, and may flow down to the secondary cylinder 15 while being discharged downward through the plurality of holes of the slurry guide 20.

That is, when the slurry flows through the slurry inlet 16, the slurry flows along the inner wall of the primary cylinder 14 of the evaporator 11, and the slurry that flows through the inner wall of the primary cylinder 14 as described above. It is heated or maintained at a constant temperature while being kept in a form accumulated in the slurry guide 20.

The slurry in such a state may be filled with a certain amount by the slurry continuously introduced into the primary cylinder 14 through the slurry inlet 16, and may continue to be discharged through the hole. The slurry can flow down evenly along the inner wall of the secondary cylinder 15 while being discharged downward through a plurality of holes formed evenly along the guide circumference.

In particular, the reactant guide 19 in the form of a spring is provided inside the secondary cylinder 15, and the slurry (reactant) released from the primary cylinder 14 side is the inner wall of the cylinder and the spring in the center thereof (hereinafter " The reaction proceeds as it flows through the reaction section, which is heated to a predetermined temperature.

That is, as described above, it is possible to determine the inflow state of the reactants flowing into the reaction section by the double-cylindrical cylinder shape. As described above, the reactants flowing into the reaction section gradually form a thin film in the reaction section. It can flow down.

At this time, the speed of the reactant flowing through the reaction section can be slowed down.

That is, the falling speed of the reactant flowing along the reaction section can be set slowly by changing the length of the spring, which in turn increases the time the reactant stays in the reaction section due to the descending nature of the spring. Allow the reaction to occur sufficiently.

At this time, the reaction temperature of the reactants reacted in the reaction section is suitable to maintain the temperature to the extent that the waste styrofoam can flow smoothly, specifically, the reaction temperature of the reactants is suitable 240 ~ 280 ℃.

If the reaction temperature is less than 240 ℃, the evaporation of the solvent is not well evaporated in the reaction zone, the falling rate is increased and discharged to the outside, if the temperature exceeds 280 ℃ during the reaction conditions, a part of the polystyrene may be pyrolyzed to generate oil Since there existed, the range was limited to 240-280 degreeC.

The solvent gas generated through the reaction section as described above is evaporated through the gas outlet 17 of the upper part of the evaporator and sent to the heat exchanger 12, and the remaining polystyrene residue is continuously discharged through the residue outlet 18 of the lower part of the evaporator. The polystyrene residue can be recovered to the residue storage tank 25 through the operation of the valve 24.

In addition, the nitrogen gas injector 21 is installed on the lower side of the reaction section so that the gas generated by the pyrolysis reaction as described above can be easily discharged to the heat exchanger 12 side. In (), nitrogen (N ₂ ) gas is injected at a flow rate of 20 to 40 ml / min to be discharged together with the solvent gas, and as a result, serves to help discharge of the solvent gas.

In particular, at the position facing the gas injection port of the nitrogen gas injector 21, a diffusion cone 23 is formed to be supported on the cylinder wall or the like, so that the solvent gas may be more actively discharged due to the diffusion of the gas.

At this time, when the injection amount of the nitrogen gas is less than (or greater than) 20 ml / min, the production rate of toluene condensed in the heat exchanger is reduced, and when the injection rate exceeds 40 ml / min, the pyrolysis gas is not sufficiently condensed in the heat exchanger. Because of this, there is a problem that the recovery rate of the solvent is lowered and odor is generated.

Meanwhile, as described above, the solvent gas discharged through the evaporator 11 is introduced into the heat exchanger 12, and the heat exchanger 12 cools / condenses the solvent gas to recover the solvent in the liquid state. .

Finally, the liquid solvent produced through the heat exchanger 12 as described above is collected in the recovery tank 4.

Hereinafter, the present invention will be described in more detail with reference to the following examples, which should not be construed as limiting the invention thereto.

Example 1

Waste styrofoam used in the present invention was used for the packaging of discarded home appliances.

As described above, the waste styrofoam was arbitrarily broken into irregular sizes, and melted with toluene at a concentration of 40%.

The reaction was introduced into the reactor at a feed rate of 5-8 mL / min through a slurry reservoir of 25 L dropping funnel.

At this time, the reactant was injected into the reactor, that is, the evaporator, the first cylinder portion at 170 ° C., and when the reactant reached a certain level, the reactant was injected into the second cylinder part at 240 ° C. and flowed down along the wall of the reaction section and the spring in the center. It was made to react.

The toluene recovered by condensing the toluene gas generated by the above reaction through a heat exchanger was collected in a recovery tank.

The recovered toluene was measured in volume using a measuring cylinder, and the recovery rate was calculated for the toluene content of 60% of the reactant injection amount, and the results are shown in Table 1 and FIG. 3.

Example 2

Waste styrofoam used in the present invention was used for the packaging of discarded home appliances.

As described above, the waste styrofoam was arbitrarily broken into irregular sizes, and melted with toluene at a concentration of 40%.

The reaction was introduced into the reactor at a feed rate of 5-8 mL / min through a slurry reservoir of 25 L dropping funnel.

At this time, the reactant was injected into the primary cylinder portion at 170 ° C. in the reactor, and when the reactant reached a certain level, the reactant was injected into the secondary cylinder portion at 250 ° C. to flow along the wall of the reaction section and the spring at the center. It was.

The toluene recovered by condensing the toluene gas generated by the above reaction through a heat exchanger was collected in a recovery tank.

The recovered toluene was measured in volume using a measuring cylinder, and the recovery rate was calculated for the toluene content of 60% of the reactant injection amount, and the results are shown in Table 1 and FIG. 3.

Example 3

Waste styrofoam used in the present invention was used for the packaging of discarded home appliances.

As described above, the waste styrofoam was arbitrarily broken into irregular sizes, and melted with toluene at a concentration of 40%.

The reaction was introduced into the reactor at a feed rate of 5-8 mL / min through a slurry reservoir of 25 L dropping funnel.

At this time, the reactant was injected into the primary cylinder portion at 170 ° C. in the reactor, and when the reactant reached a certain level, the reactant was injected into the secondary cylinder portion at 260 ° C. to flow along the wall of the reaction section and the spring at the center. It was.

The toluene recovered by condensing the toluene gas generated by the above reaction through a heat exchanger was collected in a recovery tank.

The recovered toluene was measured in volume using a measuring cylinder, and the recovery rate was calculated for the toluene content of 60% of the reactant injection amount, and the results are shown in Table 1 and FIG. 3.

Example 4

Waste styrofoam used in the present invention was used for the packaging of discarded home appliances.

As described above, the waste styrofoam was arbitrarily broken into irregular sizes, and melted with toluene at a concentration of 40%.

The reaction was introduced into the reactor at a feed rate of 5-8 mL / min through a slurry reservoir of 25 L dropping funnel.

At this time, the reactant was injected into the primary cylinder at 170 ° C. in the reactor, and when the reactant reached a certain level, the reactant was injected into the secondary cylinder at 270 ° C. to flow along the wall of the reaction zone and the spring at the center. It was.

The toluene recovered by condensing the toluene gas generated by the above reaction through a heat exchanger was collected in a recovery tank.

The recovered toluene was measured in volume using a measuring cylinder, and the recovery rate was calculated for the toluene content of 60% of the reactant injection amount, and the results are shown in Table 1 and FIG. 3.

Example 5

Waste styrofoam used in the present invention was used for the packaging of discarded home appliances.

As described above, the waste styrofoam was arbitrarily broken into irregular sizes, and melted with toluene at a concentration of 40%.

The reaction was introduced into the reactor at a feed rate of 5-8 mL / min through a slurry reservoir of 25 L dropping funnel.

At this time, the reactant was injected into the primary cylinder portion at 170 ° C. in the reactor, and when the reactant reached a certain level, the reactant was injected into the secondary cylinder portion at 280 ° C. to flow along the wall of the reaction section and the spring at the center. It was.

The toluene recovered by condensing the toluene gas generated by the above reaction through a heat exchanger was collected in a recovery tank.

The recovered toluene was measured in volume using a measuring cylinder, and the recovery rate was calculated for the toluene content of 60% of the reactant injection amount, and the results are shown in Table 1 and FIG. 3.

      Reaction temperature (secondary cylinder temperature)          Recovery of Solvent (wt%)                 240 ℃                 63.0                 250 ℃                 78.1                 260 ℃                 87.0                 270 ℃                 89.5                 280 ℃                 90.0

As described above, the present invention provides a new type of evaporation system that can efficiently recover solvents, such as easy recovery of solvents and a high recovery rate of solvents in a short time, and thus, fish farms, waste disposal plants, agricultural and fishery markets, and construction sites. In addition, the solvent can be efficiently recovered and recycled from the slurry of waste styrofoam, which is discharged in large quantities from the electronic shopping mall, and the like, so that the recycling rate of waste resources can be increased and economic and environmental effects can be expected.

Claims (7)

Slurry reservoir 10 for supplying the waste styrofoam slurry melted in the solvent, evaporator 11 for the reaction of the waste styrofoam slurry, heat exchanger 12 for the liquefaction of the evaporated gas, recovery tank for the recovery of the solvent (13) The evaporator 11 is a primary cylinder 14 and the secondary cylinder 15 and integrally formed on the top and bottom, having different diameters, and the primary cylinder 14 Slurry inlet 16 and gas outlet 17 formed in the upper portion of the upper, the residue outlet 18 formed in the lower portion of the secondary cylinder 15, and the concentric in the inside of the secondary cylinder (15) It is arranged to extend along the longitudinal direction while being configured to include a spring-like reactant guide 19 which can increase the residence time of the reactant, the boundary between the primary cylinder 14 and the secondary cylinder 15 In the slurry can hold a certain amount of guide A cone-shaped slurry guide 20 having a plurality of holes formed evenly along the circumference is provided to allow the slurry to flow down evenly along the inner wall of the secondary cylinder while the slurry is discharged downward through the plurality of holes. Apparatus for recovering the solvent from the waste styrofoam slurry, characterized in that. The apparatus of claim 1, wherein a reactant guide (19) for retention of the reactant is provided at the center of the secondary cylinder section. delete The apparatus of claim 1, wherein the secondary cylinder (15) further comprises a nitrogen gas injector (21) for assisting in the discharge of the gas produced by the reaction. 2. The solvent inlet of claim 1, wherein the slurry inlet 16 of the primary cylinder 14 is provided with a confirmation window 22 for observing the inflow of the waste styrofoam slurry applied by the solvent. Recovery device. The apparatus of claim 1, wherein the temperature of the primary cylinder is maintained at 150 to 200 ° C. 3. The apparatus of claim 1, wherein the temperature of the secondary cylinder is maintained at 240 to 280 ° C. 3.

Images