KR20040048368A - Method and apparatus for reclaiming oil from plastic - Google Patents

Abstract

The present invention provides an emulsification method and an emulsification plant for plastics capable of completely thermally decomposing large quantities of plastics as raw materials and treating hazardous gases. The plastic, which is a raw material, is dissolved in the melting part 31 to form a foamed plastic, and the foamed plastic is inclined first stage decomposition cylinder 47 having a predetermined temperature distribution and a second stage adjacent thereto. The secondary decomposition gas is decomposed to a light secondary decomposition gas which is sent to the decomposition tank 48 and depolymerized, and the extracted secondary decomposition gas is cooled and emulsified by the condensers 37 and 38 to be recovered to the oil storage tanks 42 and 43.

Description

Emulsification method of plastic and emulsification plant {METHOD AND APPARATUS FOR RECLAIMING OIL FROM PLASTIC}

Various emulsification plants for collecting oil from waste plastics have been proposed, but neither have sufficient decomposition and practically no plants operate practically.

Therefore, the present applicant has first developed an emulsification plant of a compact and simple structure of a reverse heat gradient system disclosed in Japanese Patent Laid-Open No. 2000-16774.

However, in the above emulsification plant, 1) the plastic can be reliably emulsified when the amount of plastic is low, but it is difficult to emulsify the complete plastic when the amount of plastic is increased, and 2) dissolve the polyvinyl chlorid (PVC) plastic. Hydrogen chloride gas is generated in the dissolving unit at this time, but there is a problem that the hydrogen chloride gas is not sufficiently treated and 3) the unemulsified off gas is not sufficiently processed.

The present invention has been made mainly in view of these problems, and provides an emulsification method and emulsification plant capable of emulsifying a large amount of plastic, treating hydrogen chloride gas, and completely treating off gas. It is for the main purpose.

The present invention relates to a method for emulsifying plastics and an emulsifying plant for collecting oil from the plastics.

1 is a block diagram showing the basic principle of the present invention,

2 is a block diagram showing an embodiment based on the basic principle of the present invention,

3 is a perspective view of an emulsification plant showing one embodiment of the present invention,

4 is a front view of an emulsification plant showing one embodiment of the present invention,

5 is a plan view of an emulsification plant showing one embodiment of the present invention,

6 is a schematic configuration explanatory diagram of FIG. 5,

7 is a schematic configuration explanatory diagram of FIG. 4,

8 is a cross-sectional view of the melting container,

9 is a cross-sectional view of the digester,

10 is a block diagram of a dechlorination unit,

11 is a configuration diagram of the off-gas treatment unit,

12 is a schematic configuration explanatory diagram showing another embodiment;

13 is a configuration diagram of a junction of a dissolution unit and a decomposition unit;

14 is a view showing the recovery rate according to the plastic to be treated,

15 is an explanatory view of a state in which the foam plastic is lifted up,

16 is a cross sectional view of a hopper,

17 is a perspective view of a non-heating unit,

18 is a configuration diagram of a sludge tank,

19 is a configuration diagram of the expansion barrel,

20 is a schematic configuration diagram of an accident prevention system and a deodorization system,

21 is a schematic block diagram showing another embodiment.

Thus, the emulsification method of the present invention is characterized in that the plastic is heated and dissolved to generate a foamed plastic, and the foamed plastic is taken out, heated, depolymerized and cooled to produce oil. At this time, the bubble-shaped plastic may be taken out by tilting upwards, preferably at an angle of 25 to 30 ° with respect to the horizontal. In addition, it is preferable to heat the foamed plastic while lifting it upwardly inclined, and to heat it at a higher temperature as the foamed plastic is positioned upward. Furthermore, vegetable oil, animal oil or mineral oil may be added to the dissolved plastics and heated to produce a foamed plastic composed of a mixture thereof.

In the emulsification method of the present invention, the hydrogen chloride gas generated when dissolving the plastic may be separated from other decomposition gases and then reacted with slaked lime to recover as calcium chloride. In addition, the off-gas not emulsified may be treated by contact decomposition with a high temperature ceramic.

In addition, the emulsification plant of the present invention is characterized in that it comprises a melting portion for heating and dissolving the plastic to produce a foamed plastic, and a decomposition portion for taking out the foamed plastic, heating, depolymerization and cooling to produce oil. do. In the said emulsification plant, the decomposition | disassembly part may be equipped with the taking-out means which raises a bubble-shaped plastic upwards in inclination, Preferably it takes out at an angle of 25-30 degree with respect to a horizontal. The decomposing unit may be heated while lifting the bubble-shaped plastic upwardly inclined, and heating means for heating at a high temperature as the bubble-shaped plastic is positioned upwards. Furthermore, an oil injection means for injecting vegetable oil, animal oil or mineral oil may be provided at the junction between the dissolution unit and the decomposition unit. The melting portion may be formed of a plurality of melting vessels having different temperature distributions, and the dissolving portion may be formed of a plurality of inclined decomposition vessels having different temperature distributions.

Furthermore, the emulsification plant of the present invention may include a dechlorination apparatus for treating hydrogen chloride gas generated in the dissolution unit, and the dechlorination apparatus includes a separator for decomposing hydrogen chloride gas and other decomposition gases, and hydrogen chloride separated by a separator. It is preferable to provide a reactor in which the gas is reacted with slaked lime to form calcium chloride. In addition, the off-gas processing apparatus which contacts-decomposes and processes off gas which is not produced | generated with oil after cooling in a decomposition part by high temperature ceramic may be provided.

In addition, the emulsion plant of the present invention may be provided with a residue recovery means at the upper end of the decomposition tank of the final stage of the digestion tank provided in multiple stages, the residue recovery means is located in the upper position of the decomposition tank of the final stage The lower opening may be formed by a cylinder placed in an inert gas atmosphere that is heavier than air.

Furthermore, the emulsification plant of the present invention preferably includes a hopper for storing plastic and supplying it to the melting part, and the hopper preferably includes a lead screw having a spiral wing. Moreover, what is necessary is just to provide the non-heating part formed in the non-heated area | region of predetermined length between a hopper and a melting part. Furthermore, the plurality of melting cylinders are provided with lead screws having spiral blades for conveying plastics, and if the pitch of the lead screw blades of the melting cylinders located at the top is larger than the pitch of the blades of the lead screws of the other melting cylinders, good.

Further, the emulsification plant of the present invention is a temperature for detecting the temperature of the melting section and the decomposition section of the inner cylinder and the outer cylinder formed on the outer periphery of the inner cylinder, the hot air space through which the hot air formed between the inner cylinder and the outer cylinder is circulated; A carbon dioxide gas supply device may be provided that includes a sensor and further supplies a carbon dioxide gas to the hot air space when the temperature sensor detects an abnormal temperature that is equal to or higher than a predetermined temperature.

Further, the emulsification plant of the present invention is configured to include a dissolution portion and a decomposition portion with an inner passage, an outer cylinder formed on the outer circumference of the inner cylinder, and a hot wind space formed between the inner cylinder and the outer cylinder to circulate hot air, A hot air generator for generating hot air to be supplied to the furnace by combustion, and a drying device for drying the plastic to be supplied to the melting furnace, and supplying air in the drying device to the hot air generator for deodorization by combustion. In addition, the air in the drying apparatus may be supplied to the off-gas treatment apparatus to be decomposed by contact decomposition with a high temperature ceramic.

Further, the emulsion plant of the present invention uses a telescopic cylinder freely stretched to a part of the dissolution tank, the telescopic cylinder is disposed in the inner cylinder and the outer periphery of the inner cylinder, one end is fixed to the inner cylinder and the other end to the inner cylinder What is necessary is just to form the slidable bellows and the outer cylinder fixed to the other end of the said bellows, and the inner cylinder slidably accommodated inside.

Further, the emulsifying plant of the present invention is formed with a heat medium space formed between an inner cylinder, an outer cylinder formed on the outer circumference of the inner cylinder, an inner cylinder and an outer cylinder, and a liquid heat medium circulated therein, A thermal medium supply device for supplying a liquid thermal medium to the media space may be further provided.

EMBODIMENT OF THE INVENTION Hereinafter, embodiment of this invention is described with reference to drawings.

1 is a conceptual diagram for explaining the basic principle of the emulsification method of the plastic according to the present invention. Plastic, which is a raw material, is dissolved at a temperature of 200 ° C to 350 ° C and stored in the storage unit 1. And the melted plastic (dissolving plastic) is pulled up in the inclination upward by the disassembly cylinder 13.

Here, the decomposition cylinder 13 is comprised with the inner cylinder 2, the outer cylinder 6 which forms the hot air space 4 around the said inner cylinder 2, and the lead screw 7. As shown in FIG. The lead screw 7 is composed of a rotating shaft 14 and a spiral blade 8, and is rotated at a speed of 4 to 5 revolutions / minute by the motor 12. In addition, hot air is supplied to the hot air space 4 from the pipe 10, and the temperature in the inner cylinder 2 is maintained at 350 to 620 ° C. because the gas is depolymerized by plasticizing the plastic.

The molten plastic conveyed in the inner cylinder 2 by the lead screw 7 is firstly decomposed (first heavy gas state gasified in the dissolved state) under the decomposition cylinder 13 to become the primary decomposition gas. Further, the primary cracked gas is sent out at a low speed above the cracking cylinder 13 by the lead screw 7 and in the inner cylinder 2 maintained at 350 ° C to 620 ° C by hot air supplied from the pipe 15. Secondary decomposition (the state in which plastic is depolymerized and emulsified when cooled) becomes light secondary decomposition gas.

In addition, if the secondary decomposition of all the oil components contained in the plastic, which is a raw material, is performed at the top of the decomposition cylinder, one decomposition tank is sufficient, but the first stage is connected to the storage unit 1 using two decomposition cylinders. It is also possible to set it as a disassembly cylinder, and to connect a 2nd stage decomposition cylinder to the said 1st stage decomposition cylinder.

In addition, since the hot air space 3 is formed outside the storage unit 1, an outer box 5 is formed, and hot air is sent to the hot air space 3. The plastic supplied to the storage part 1 is heated to 200-350 degreeC, and becomes melted plastic (mp), and forms foam-shaped plastic (foam plastic, f) in the surface part. The foamed plastic f is heated while being obliquely lifted by the lead screw 7 in which the shaft end 14a is deposited in the molten plastic mp, but at this time, the contact area with heat becomes large, so that it is reliably decomposed ( Depolymerized to form secondary cracked gas. The secondary cracked gas is collected in the pipe 9, emulsified by cooling, and recovered to the oil storage tank.

In addition, it is preferable that the speed of lifting up the frothed plastic f is 30 to 60 cm / min, and if it is less than this, the conveyance efficiency becomes worse, and when it exceeds this, sufficient disassembly becomes impossible. For example, although the foam plastic f is helically lifted by the lead screw 7, as shown in FIG. 15, the speed of moving to the spiral shape at this time is preferably 30 to 60 cm / minute. This speed is controlled by, for example, the pitch p of the lead screw 7. In this way, the foamed plastic f is sufficiently decomposed (depolymerized) in the primary decomposition temperature region and the secondary decomposition temperature region by conveying the inside of the inner cylinder 2 at the above-mentioned speed and gradually heating. It is preferable to heat the foam plastic (f) for about 14 to 15 minutes until the secondary decomposition is completed at around 600 ° C.

The treatment temperature varies depending on the type of plastic, which is a raw material. However, the temperature of the storage part 1 is preferably set at a temperature (200 to 350 ° C.) in which the plastic (mp) is foamed. It is important to make the inclination smooth and keep the bubble state long so as to make the contact area with heat large. For this purpose, the disassembly cylinder 13 is preferably inclined with respect to the horizontal. In addition, the inside of the inclined decomposition cylinder 13 blows hot air upward and circulates from the top to the bottom, so that the temperature gradually rises from the bottom to the top. This method is called a so-called hot air gradient method.

In order to keep the foamed plastic f well for a long time, it is preferable to set the inclination angle θ of the decomposition cylinder 27 to 25 ° to 30 ° as shown in FIG. 2. If the inclination angle θ of the decomposition cylinder 27 is less than 25 °, the foamed plastic f flows quickly horizontally to turn off in a short time, and if the inclination angle θ is set to more than 30 °, the melted plastic in relation to gravity It is difficult to pull up the frothed plastic f upward long distance from the surface of (mp), and also in this case, the frothed plastic f turns off in a short time.

In FIG. 2, the storage part 29 of molten plastic (mp) is formed in the connection part in which the supply cylinder 28 and the decomposition cylinder 27 were connected in V shape. The supply cylinder 28 consists of the inner cylinder 20 and the outer cylinder 21, hot air is supplied through the piping 22 between them, and the inner cylinder 20 is maintained at 200-350 degreeC.

Disassembly cylinder 27 consists of the inner cylinder 25, the outer cylinder 17, and the lead screw 24, the lead screw 24, the lower end of the shaft 23 is rotatable on the lower wall of the storage unit 29 To be supported. Between the inner cylinder 25 and the outer cylinder 17, the heating air of 450-620 degreeC is supplied through the piping 26c in a hot-air generation furnace. Then, the heated air descends the inside of the decomposition cylinder 27 and is withdrawn from the pipe 26b at the lower part of the decomposition cylinder, and circulated so as to flow into the upper pipe 26a. As the hot air circulates from the top to the bottom in the cracker 27 in this manner, the temperature distribution in the cracker 27 is formed so that the temperature rises from the bottom to the top. The lower part of the decomposition cylinder 27 is maintained at 300 to 450 ° C because it performs primary decomposition, and the upper part of the decomposition cylinder 27 is heated to around 600 ° C because secondary decomposition is performed.

The liquid state plastic f is generated in the storage portion 29, and the liquid state plastic f is conveyed to ascend the inside of the inclined decomposition tank 27 in a good state, and is heated during the conveyance to become cracked gas. The cracking cylinder 27 and the supply part 28 are connected in a V-shape, and since the storage part 29 is completely closed in melted plastic mp, the cracking gas from the cracking container 27 to the supply container 28 is carried out. It is safe without backflow, and also prevents air from entering the cracking bin 29 from the outside through the storage unit 29 and there is no risk of explosion.

Next, an emulsification plant to which the emulsification method of the plastic is applied will be described.

3 to 7, in the emulsification plant 30 of the present invention, for example, the dissolution unit 31 for dissolving waste plastics as a raw material and the plastic dissolved in the dissolution unit 31 are firstly decomposed and displaced. A decomposing unit 32 for decomposing the car, a dechlorination unit 33 for dechlorination when treating PVC containing chlorine, and an off gas processing unit 34 for processing off gas generated during dissolution and decomposition of plastics. ) And first and second hot weathering furnaces 35 and 36 for generating hot air as a heat source during dissolution and decomposition.

As shown in FIG. 6, the melting part 31 has the 1st melting container 31a which connects the hopper 41 which inject | pours plastic which is a raw material through the non-heating part 410, and the 1st melting container 31a. Of the second melting cylinder 31b orthogonal to the first melting cylinder 31a and the rear end thereof connected to the lower side of the second melting cylinder 31b. And a third melting cylinder 31c orthogonal to 31b) and a fourth melting cylinder 31d connected to the rear end of the third melting cylinder 31 below the front end and orthogonal to the third melting cylinder 31c. It is composed. Thus, the 1st-4th melting cylinders 31a, 31b ... 31d are arrange | positioned as a rectangle as a whole, and the plastic melt | dissolved from the front end of a decomposition tank to the rear end of the next melting tank is sequentially sent out. In addition, these melting cylinders 31a-31d may be connected horizontally.

As shown in FIG. 16, the hopper 41 includes a rod-shaped casing 411, a lid 412 covering the upper surface of the casing 411, a motor 413 disposed in the center of the lid 412, and And a lead screw 414 composed of a rotating shaft 414a connected to the motor 413 and extending into the casing 411 through the cover 412 and a spiral blade 414b attached to the rotating shaft 414a. do. The spiral blade 414b of the lead screw 414 has a rod shape so as to conform to the shape of the casing 414 as a whole. And the space | interval W of about 2-5 cm is provided between the inner wall of the casing 414, and the outer periphery of the spiral blade 414b. The lead screw 414 is rotated at a predetermined speed by the motor 413 to prevent the light plastic from clogging the hopper 41. Then, the heavy plastic falls through the gap W between the inner wall of the casing 414 and the outer circumference of the spiral blade 414b, and the light plastic scrap is reliably into the unheated portion 410 by the lead screw 414. It is sent out.

The non-heating part 410 is formed in a cylinder and is connected to the lower part of the hopper 41 (refer FIG. 17). A motor 42 is provided at an end portion of the non-heating portion 410, and a lead screw 137 common to the lead screw 137 disposed in the melting vessel 31a to be described later is connected to the motor 42. The lead screw 137 is rotated by the motor 42, and slowly sends the small pieces of plastic sent out from the hopper 41 to the front, and supplies them to the melting container 31a. In addition, unlike the melting cylinder 31 mentioned later, the non-heating part 410 does not heat by warm air. Therefore, since the attachment part of the hopper 41 and the melting cylinder 31 are spaced apart, dissolution of the plastic does not start in the vicinity of the attachment part of the hopper 41, and the lead screw 137 of the lead screw 137 is caused by the viscous resistance of the dissolved plastic. The rotation can be prevented from stopping. That is, by dissolving the dissolving portion of the plastic from the attachment portion of the hopper 41, the dissolving plastic portion is lengthened, and the dissolving plastic is pushed into the undissolving plastic.

The melting container 31 is comprised from the rectangular outer box 136 and the inner cylinder 131 provided in the outer box 136 (FIG. 8). In the inner cylinder 131, a lead screw 137 having a rotating shaft 133 and a spiral blade 132 provided around the rotating shaft 133 is provided. The lead screw 137 of the first melting cylinder 31a has a larger pitch than the lead screws 137 of the other melting cylinders 31b, 31c, and 31d. This is because, as will be described later, since the set temperature of the first melting cylinder 31a is lower than that of the other melting cylinders, the resistance is reduced to lower the convection density of the plastic. The lead screw 137 is rotated by the motor, for example, the first melt cylinder 31a is rotated by the motor 42, Figs. 4 and 5, and the second melt cylinder 31b is the motor 55. Is rotated.

In addition, the inner cylinder 131 is provided with a plurality of endothermic blades 134 on the outer circumference. In addition, a hot air space 135 is formed between the inner cylinder 131 and the outer box 136. The 1st melting tank 31a is adjusted to 190-200 degreeC, the inside of the 2nd melting tank 31b is adjusted to 210-230 degreeC, the 3rd melting tank 31c is adjusted to 230-260 degreeC, and the 4th The dissolution tank 31d is adjusted to 300-340 degreeC. In this way, the four melting cylinders 31a, 31b, and 31d are arranged in a rectangular shape and the temperature of each melting cylinder is gradually increased to a) reliably dechlorination of plastics containing chlorine such as vinyl chloride. In order to ensure sufficient convection time (for example, 20 minutes), b) to smooth the temperature distribution by multiplexing, to facilitate temperature control, and c) of the first melting vessel 31a. This is to lower the temperature, to prevent welding of the plastic to the rotary shaft 133 in the vicinity of the hopper 41, and d) to shorten the design length of the entire plant.

In addition, hot air is supplied into each melting cylinder 31 via the piping 70 in the 1st hot weathering furnace 35, and the hot air is sent toward the upstream side from the downstream side through which plastic is sent out. Therefore, each melting cylinder 31 has a reverse heat gradient. Circulation of the hot air in each melting cylinder 31 is performed by the blowers 56, 57, 58 (FIGS. 4, 60; FIG. 7). In addition, a communication 59 is connected to the first and second hot wind generating furnaces 35 and 36. The communication 59 has branch pipes 59a and 59b and an outlet 59c, and is formed in an inverted U shape (Fig. 4).

The disintegrating unit 32 is provided near the first stage decomposition cylinder 47 and the first stage decomposition cylinder 47 controlled at 350 to 420 ° C., and the second stage decomposition cylinder 48 controlled at 450 to 580 ° C. It consists of (FIG. 7). And the decomposition cylinders 47 and 48 are installed inclined at 25-30 degreeC with respect to a horizontal plane. The tip end of the fourth melting cylinder 31d is connected in the first stage decomposition cylinder 47, and the connecting portion forms a storage portion of the dissolved plastic.

The first stage decomposition cylinder 47 is composed of two unit decomposition cylinders 47a and 47b partitioned by the partition plate 256 and formed in two rows at the left and right (FIG. 9). The unit decomposition cylinders 47a and 47b include an inner cylinder 255, a plurality of heat absorbing fins 253 provided on the outer circumference of the inner cylinder 255, a lead screw 150, and a thermal space 254 through which hot air is sent. It is provided. Each lead screw 150 is composed of a rotating shaft 251 and a spiral blade 252 is rotated by the motor (51, 52 (Fig. 5)).

The second stage decomposition cylinder 48 has substantially the same structure as the first stage decomposition cylinder 47, and the inner cylinders 148 are provided in the unit decomposition cylinders 48a and 48b (FIG. 6), respectively. A lead screw 149 is provided in the inner cylinder 148, and the lead screw 149 is rotated slowly (4 to 5 revolutions / minute) by the motors 53 and 54 (FIGS. 5 and 7).

At the upper end of the inner cylinder 255 of the first stage decomposition cylinder 47, a super heater 151 for heating the decomposition gas passing through to 580 ~ 620 ℃ is provided (Fig. 7). The decomposition gas secondaryly decomposed in the first stage decomposition cylinder 47 is drawn out through the super heater 151 and the pipe 49, and the condenser 37 (FIG. 5) via the scrubber 60 for alkali cleaning. Are sent). The cracked gas is cooled in the condenser 37 and emulsified, and the oil is stored in the oil storage tank 42 through the pipe 46. A part of the oil stored in the oil storage tank 42 is supplied to the hot air generating furnaces 35 and 36 via the service tank ST1.

In the middle of the pipe 49, a valve 49a for adjusting the flow rate of the decomposition gas flowing in the pipe 49 is attached. It is necessary to send only the light cracked gas which was completely secondaryly decomposed by the first cracker 47 to the condenser 37, but slightly heavy imperfection of secondary gas which is not completely decomposed in the cracked gas derived from the pipe 49. Contains cracked gases. And, when the amount of decomposed gas in the pipe 49 is small, the incomplete decomposed gas cannot exceed the generation part of the pipe 49, and is returned to the first stage decomposition cylinder 47 to intervene the dropping cylinder 120. Although sent to the second stage decomposition cylinder 48, when the amount of decomposed gas from the pipe 49 increases, the derivation moment of the decomposed gas increases, and the incomplete decomposed gas also exceeds the generation portion of the pipe 49, and the condenser 37 Are sent). Therefore, the amount of decomposed gas drawn out from the pipe 49 is adjusted by the valve 49a to prevent the incomplete decomposed gas from being sent to the condenser 37.

Since the first stage cracker 47 is adjusted to 350 to 420 ° C. as described above, in the first stage cracker 47, a part of the oil component corresponding to gasoline having low decomposition temperature, kerosene and diesel oil equivalent component is firstly. After decomposition, it is secondary decomposition. Here, the gas in an insufficient decomposition state is completely secondary decomposition in the super heater 151. The secondary decomposition cracked gas is cooled and emulsified in the condenser 37. The gas that is not sufficiently emulsified in the condenser 37 is sucked through the pipe 46 having the pump P, and is recovered as the off gas into the oil storage tank 42.

The plastic component of the oil state which is not completely disintegrated in the 1st stage decomposition container 47 is supplied to the lower end of the 2nd stage decomposition cylinder 48 via the dropping cylinder 120, and the 2nd stage decomposition cylinder The lead screw 149 in 48 is sent upwardly inclined. Since the second stage cracking cylinder 48 is adjusted to a temperature of 450 to 580 ° C., the second stage cracking cylinder 48 also completely decomposes the remaining portions of kerosene, light oil equivalent components, and heavy oil components. Residues such as metal, mud and the like introduced together with the plastic are recovered to the sludge tank 40 via the sludge pipe 40a.

In the sludge tank 40, as shown in Fig. 18, water 40b is stored, the metal mesh 40c is provided in the water 40b, and the residue is recovered on the metal mesh 40c. By taking out the metal net 40c from the sludge tank 40, a residue can be taken out from the sludge tank 40. FIG. The upper surface of the sludge tank 40 is covered with a lid 40d having an opening 40e in part. Water 40b of the sludge tank 40 is filled with an inert gas 40f that is heavier than air such as carbon dioxide gas, and the lower end of the sludge tube 40a is located in the inert gas 40f. A gas cylinder 40g is connected to the sludge tank 40, and an inert gas 40f is supplied from the gas cylinder 40g into the sludge tank 40. An inert gas 40f supplied from the gas cylinder 40g. A part of is overflowing from the opening 40e. Thus, by placing the lower end of the sludge tube 40a in the inert gas 40f, the air in the second stage decomposition pipe 48 in the sludge tube 40a is Inflow can be effectively prevented and there is no risk of explosion In addition, when the lower end of the sludge tube 40a is placed in the water 40b, a light residue floats due to the buoyancy of the water, and the lower end of the sludge tube 40a. Although the part is clogged, this is prevented by placing the lower end of the sludge tube 40a in the inert gas 40f so that the residue smoothly falls into the water 40b.

Hot air is supplied to the upper part of the first stage and the second stage crackers 47 and 48 via the pipes 71, 71a, and 71b (FIG. 5) from the second hot wind generating furnace 36d, and the hot wind is a cracker. It is circulated in the blowers 170 and 171 by exiting from the lower part of 47 and 48 and returning to the upper part. In this way, the decomposition cylinders 47 and 48 are formed in a reverse heat gradient that becomes low from the top to the bottom. In addition, hot air from the first hot wind generating furnace 35 is supplied to the melting part 31, and the hot air is circulated by the blower 60 in the fourth melting cylinder 31d (FIG. 7).

At the upper end of the inner cylinder 148 of the second stage decomposition cylinder 48, a pipe 50 connected to the condenser 38 via the scrubber 61 for alkaline cleaning is disposed (FIG. 5). The cracked gas decomposed in the second stage cracker 48 is sent to the scrubber 61 through the pipe 50 and further to the condenser 38. The cracked gas sent to the condenser 38 is emulsified by cooling. The emulsified oil is sent to the oil storage tank 43 by the pipe 86, and moreover, a part of the oil is sent to the first and second hot air generating furnaces 35 and 36 via the service tank ST2. Lose. In addition, the capacitors 37 and 38 are cooled by a cooling tower CT (FIG. 3).

Pipes 101 and 102 connected to the collective exhaust pipe 100 are connected to the first and second stage disassembling cylinders 47 and 48. In addition, the exhaust of the first stage and the second stage decomposition cylinders 47 and 48 is discharged to the outside from the collective exhaust pipe 100 via the pipes 101 and 102. In addition, the gas which is not emulsified by the capacitor | condenser 38 connected to the said 2nd stage decomposition tank 48 is collect | recovered to the oil storage tank 43 through the piping 86 by the pump P. As shown in FIG.

The expansion cylinder 700 is used for a part of the melting cylinder 31 and the decomposition cylinders 47 and 48 which were demonstrated above. The telescopic cylinder 700 is formed of a bellows portion 701 and a slide portion 702 (FIG. 19). The bellows portion 701 is composed of a bellows 703 and a bellows inner cylinder 704 disposed therein, and the entire length of the bellows inner cylinder 704 is longer than the full length of the bellows 703. The bellows 703 and the bellows inner cylinder 704 are provided with one end side, and the bellows inner cylinder 704 protrudes from the other end side of the bellows 703. And the support cylinder 705 is arrange | positioned at the outer periphery of the bellows inner cylinder 704 which protrudes, and the slide part 702 is comprised by the said bellows inner cylinder 704 and the support cylinder 705. The inner diameter of the support cylinder 705 is slightly larger than the outer shape of the bellows inner cylinder 704, and the inner circumferential surface of the support cylinder 705 and the outer circumferential surface of the bellows inner cylinder 704 form a sliding surface. 19, the inner cylinder 706 formed with the same diameter as the bellows inner cylinder 704 is arrange | positioned in the part in which the bellows inner cylinder 704 of the support cylinder 705 is not located, Furthermore, the bellows inner cylinder 704 and the inner cylinder ( At the opposite side ends of 706, corresponding ends 704a and 706a are formed. In this case, both ends 704a and 706a are formed. In this case, the opposing surfaces of both ends 704a and 706a form a sliding surface.

In this way, the expansion and contraction vessel 700 disposed in the melting vessel 31 and the part of the decomposition cylinders 47 and 48 is a case where the melting cylinder 31 and the decomposition cylinders 47 and 48 are heated and thermally expanded. To absorb the amount of expansion. That is, for example, when the first melting cylinder 31a is heated to about 200 ° C. at room temperature and the electric field is increased by thermal expansion, the expansion and contracting cylinder 700 disposed on a part of the first melting cylinder 31a is a bellows 703. In order to reduce the pressure, the bellows inner cylinder 704 is moved to the slide portion 702, and then contracted to absorb the expansion amount of the first melting cylinder 31a.

Furthermore, the expansion and contraction cylinder 700 shown in FIG. 19 provides the slide position of the bellows inner cylinder 704 to the outside of the bellows portion 701, and uses a support cylinder 705 having a larger diameter than the bellows inner cylinder 704. Since the slide portion 702 is formed, the bellows inner cylinder 704 can be thickened without reducing the inner diameter of the bellows inner cylinder 704. As a result, the deformation of the expansion and contraction cylinder 700 can be prevented, and further, the decomposition gas at the damaged portion of the bellows 703 can be prevented without damaging the bellows 703 caused by the deformation and expansion of the expansion and contraction cylinder 700. It is possible to prevent the occurrence of fire due to the outflow of the back.

Next, the detail of the dechlorination apparatus 33 is demonstrated.

Pipes 75, 76, and 77 extending from the upper surfaces of the melters 31a, 31b, and 31c of the melter 31 are connected to the pipe 78 (FIG. 5), and the pipe 78 is connected to the first separator ( 37) (FIG. 10). The first separator 37 is for separating the hydrogen chloride gas generated in the melting vessels 31a, 31b, and 31c from the decomposition gas slightly contained therein. The first separator 37 has a cooling coil 301 at the top. The hydrogen chloride gas flowing in the pipe 78 is cooled when passing through the cooling coil 301, and is discharged to the lower portion of the first separator 37 positioned below the cooling coil 301. The released hydrogen chloride gas is further sent to the second separator 38 having the same structure as that of the first separator via the cooling coil 301 through the pipe 79 at the top of the first separator 37. Further, the hydrogen chloride gas separated in the second separator 38 is sent to the third separator 39 having the same structure as the first and second separators 37 and 38, and completely separated from the decomposition gas in the third separator 39. After being separated, it is sent to the lower part of the reactor 300 via the pipe 81. By arranging these separators 37, 38, and 39, hydrogen chloride gas can be isolate | separated completely from decomposition gas.

Reactor 300 has a stirring rod 306, the wing 308 is attached to the stirring rod 306. The slaked lime tank 83 is connected to the upper portion of the reactor 300. The slaked lime tank 83 is provided with the heating cylinder 305 around it in order to dry the slaked lime in the slaked lime tank 83. A lead screw 303 is provided below the slaked lime tank 83, and the lead screw 303 is rotated by the motor 304.

In addition, a lead screw 309 is provided at a lower end of the reactor 303, and the lead screw 309 is rotated by the motor 310. The lead screw 309 is rotated by the motor 310. The periphery of the lead screw 309 is heated by a heating tube 313 for drying and removing water generated by the reaction of the reactor. The calcium chloride produced by the reaction in the reactor 309 is stored in the calcium chloride tank 312. Further, temperature sensors S1, S2, and S3 are provided at appropriate positions in the height direction of the reactor 300, the reaction heat is detected by the temperature sensors S1, S2, and S3, and the slaked lime tank is reacted by the reaction heat detection signal. The rotation of the motor 310 of the motor 304 and the lead screw 309 for discharging the reactor 300 is controlled. That is, the stirring rod 306 of the reactor 300 is constantly rotating, and when a large amount of hydrogen chloride gas enters the reactor 300, the reaction is vigorous and a large amount of heat of reaction is generated. And when the highest temperature sensor S3 detects reaction heat more than fixed, the lead screw 303 of the slaked lime tank 83 is rotated so that a large amount of slaked lime may be sent out. Thereafter, the reaction proceeds, the generation of heat of reaction decreases, the temperature slightly decreases, and the slaked lime is supplied accordingly while the intermediate temperature sensor S 2 detects the temperature in a predetermined range. Further, when the reaction is slowed down and the lowest temperature sensor S1 detects a predetermined temperature, it is determined that the reaction is finished, and the calcium chloride produced by rotating the lead screw 309 for discharging the reactor 300 is converted to calcium chloride. The tank 312 is recovered. After the produced calcium chloride is recovered and the reaction is started again, the temperature sensor S1 detects the start of the reaction, rotates the lead screw 303 and sends the calcined lime from the slaked lime tank 83 into the reactor 300. As the heat of reaction is sequentially detected by the temperature sensors S2 and S3, the supply of slaked lime increases, the supply amount of slaked lime decreases as the heat of reaction decreases, and the operation as described above is repeated.

Normally, it is said that hydrogen chloride gas does not react with a dry neutralizing agent without a solvent. However, when hydrogen chloride gas is reacted with slaked lime, the water generated at that time becomes a solvent and accelerates the neutralization reaction. The reaction scheme is as follows.

2HCl + Ca (OH) ₂ = CaCl ₂ + 2H ₂ O

In addition, a vacuum pump 314 is provided to remove water generated as water vapor in the reaction and to introduce hydrogen chloride gas into the reactor 300. In order to make the suction load in the vacuum pump 314 constant, a relief valve 315 for introducing air is provided at the inlet side of the vacuum pump 314. In addition, an alkali cleaning scrubber 317 is provided to remove hydrogen chloride gas that has not sufficiently reacted in the reactor 300.

Next, the off-gas processing apparatus 34 is demonstrated.

11 is a diagram illustrating a schematic configuration of the off gas treatment device 34. As shown in FIG. 11, the off-gas treatment apparatus 34 has a casing 236. And, during the operation of the emulsification plant, the burner 234 is constantly connected to the casing 236, and the casing 236 is heated to about 1200 ° C.

In the casing 236, a plurality of ceramic footnotes 238, 238, and 238 are provided. The ceramic footnotes are catalytically decomposed off gas introduced from the inlet 235 connected to the oil storage tanks 42 and 43 to 1/100 seconds to 2/100 seconds, and simple oxides such as CO ₂ , N0 _x , and H ₂ O. Change to. The heat energy generated at this time is guided to the first and second hot air generating furnaces 35 and 36 through the outlet 237.

The off gas is an environmental hormone such as acetaldehyde which is not emulsified in the condensers 37 and 38. In the present embodiment, the off gas is once recovered from the oil storage tanks 42 and 43 and then off gas treated in these oil storage tanks 42 and 43. Sent to device 34. In addition, you may send off gas to the off gas processing apparatus 34 directly from the condenser 37,38.

Next, a description will be given of the safety system and deodorization system in the inclined tube.

As shown in FIG. 20, each of the dissolution pipes of the dissolution part 31 and each of the inclination pipes of the dissolution part 32 includes a plurality of temperature sensors S, S. S is provided. Each of these sensors S is connected to the controller 511, and the controller 511 controls the opening and closing of the valve 513 connected to the carbon dioxide gas cylinder 512. The carbon dioxide gas cylinder 512 is connected to a warm air circulation path P for sending warm air from the first and second warm air generating furnaces 35 and 36 into the dissolution unit 31 and the decomposition unit 32. The controller 511 opens the valve 513 when the temperature sensor S detects an abnormal temperature such as an accident, and dissolves the portion 31 and the decomposing portion through the hot air circulation passage Q through the carbon dioxide gas. Supply within 32). Thereby, the inside of the dissolution part 31 and the decomposition | disassembly part 32 is cooled, and operation | movement of the emulsification plant 30 is stopped.

A suction device 514 having a suction fan 514a is disposed upward in the deposition field A of the plastic to be treated. In particular, the air accompanied by the off-odor generated in the waste plastic is sucked by the suction device 514, is sent to the warm air generating furnace 36, and burned and deodorized.

Further, the thin piece P of plastic pulverized by the crusher 515 is dried using the warm air in the warm air generating furnace 36 in the dryer 516, and the thin piece P of dried plastic is hopper ( Are sent to 41). Here, when the thin piece P of plastic is dried by warm air in the dryer 516, a odor may be filled in the vicinity. Thus, the air in the dryer 516 accompanied by the odor is sent to the warm air generation furnace 35 after the fine particles mixed in the air in the cyclone 517 by the fan 516a are processed. A sufficient deodorizing effect is expected by these systems.

The off-air air may be decomposed by the off gas processing unit 34 for processing off gas. That is, the air accompanied by the off-odor is processed in the warm air generating furnace (35, 36) or the off-gas processing unit 34.

In the above embodiment, although the decomposition cylinder is provided in two stages, as shown in FIG. 12, after the decomposition cylinder 48 of the 2nd stage, it is tilted at the same angle of the same structure as the 2nd stage decomposition cylinder 48. The third stage cracker 210 is provided, and each temperature distribution is 350-400 degreeC in a 1st stage digester, 400-480 degreeC in a 2nd stage digester, and 480 in a 3rd stage digester. You may provide the melting part 200 set to -580 degreeC. By using three stages of the decomposition vessel in this way, the decomposition temperature distribution can be taken more smoothly, and the decomposition time can be taken longer. Disassembly is guaranteed.

That is, the upper end side of the second stage decomposition cylinder 48 is connected to the lower end of the third stage decomposition cylinder 210 of the same inclination angle via the dropping cylinder 218, and is not extracted from the second stage decomposition cylinder 48. Undecomposed foam-like plastics and cracked gas are sent into the third stage cracking tank 210 via the dropping cylinder 218. The undecomposed foam-like plastic and the decomposition gas sent to the third stage decomposition tank 210 are secondaryly decomposed in the third stage decomposition cylinder 210, and the secondary decomposition decomposition gas is the scrubber 216 for alkaline cleaning. It is cooled and emulsified in the condenser 213 through the oil to form oil equivalent to A heavy oil. The oil is recovered to the oil storage tank 215 via the pipe 214. A blower 221 is connected to the third stage cracker 210, whereby the heated air is circulated while forming a reverse heat gradient from the top of the cracker down. In addition, the residue is recovered into the sludge tank 220 into which water is injected through the sludge pipe 219. In addition, the cracked gas that is not emulsified in the condenser 213 of the third stage cracking tank 210 is sucked by the pump P and recovered to the oil storage tank 215 through the pipe 214. In addition, although the decomposition gas 47 and 48 of the 1st stage | paragraph and the 2nd stage | paragraph are taken out and emulsified the decomposition gas secondaryly decomposed | disassembled from the upper end, at this time, the gas which was not completely secondary-decomposed was superheated (151,152) Disassemble by). In the second stage cracking cylinder, cracked gas corresponding to light oil, kerosene and some heavy oil components can be obtained, and the remaining components of A heavy oil equivalent are cracked in the third stage cracking cylinder. Moreover, it is also possible to make a decomposition cylinder four or more stages.

In addition, in the Example shown in FIG. 12, the melting part 200 is formed in a vertical shape (vertical type). That is, the first, second, and third melt cylinders 201, 202, and 203 are connected in the vertical direction via the connecting portions 204 and 205, respectively, and the plastic sent from the hopper 41 is the first melt vessel 201. Is sent in the right direction, is sent in the left direction in the second melting cylinder 202, sent in the right direction in the third melting cylinder, and supplied to the lower end of the first stage decomposition cylinder 47. The lead screw 207 of the lowermost third melt cylinder 203 is rotated by the motor 208, and the rotation of the motor 208 is through the chain 209 through the lead screw of the first melt cylinder 201. 206 is rotated, and further, the rotation of the lead screw 206 rotates the lead screw 212 of the second melt cylinder 202 via the gears G1 and G2. In addition, hot air is blown out by the blower 213 from the upper side where the temperature of the dissolution part 200 is low, and is sent downward through the piping 222, and the inside of a dissolution part is circulated upward.

In the embodiment shown in FIG. 21, the 1st-4th melt cylinder 31a, 31b ... 31d is heated by the heat medium supplied from the heat medium heating apparatus 600. In FIG. Here, the heat medium means a liquid heat medium, and various heat medium oils are used, for example. The heat medium is heated to a predetermined temperature in the heat medium heating device 600, and is supplied to the heat catalyst space 135 ′ of the melting vessel 31 through the heat medium pipe 601. The thermal catalyst space 135 ′ is formed between the inner cylinder 131 and the outer box 136 similarly to the hot air space 135 described above. The heat medium is circulated in the circulation pump 602 so that the heat medium space 135 'flows from the downstream side to the upstream side. The hot air mentioned above is controlled at 190-200 degreeC in the 1st melting tank 31a, 210-230 degreeC in the 2nd melting tank 31b, and 300-340 degreeC in the 4th melting tank 31d. The same as in the case of heating by.

Thus, by using a heat medium instead of hot air, it is possible to greatly improve a) heat transfer effect, and b) heat medium does not cool well compared with hot air, so even when the plant is stopped, the temperature in the melting tank 31 is reduced. It is possible to stand in a short time when the plant is built without going down well, and furthermore, c) it is possible to prevent the occurrence of a fire even when the inner cylinder 131 of the melting cylinder 31 is damaged.

In addition, since the operating temperature of the heat medium is generally 350 ° C. or lower, the heat medium is used only for heating the melting vessel 31, but the heat medium can also be used for heating the decomposition cylinders 47 and 48 by selecting an appropriate heat medium. Do. Moreover, only the melting tank 31, for example, the 1st, 2nd, 3rd melting tanks 31a, 31b, 31c which are adjusted to low temperature among the melting tanks 31 by the operating temperature of the heat medium to be used as a heating medium. You may heat.

In the embodiment shown in FIG. 13, the lower part of the 4th dissolution cylinder 31d and the 1st stage disassembly cylinder 47 is joined by the junction part 500, and the foamed plastic agent melt | dissolved through the said junction part 500 is carried out. It is supplied to the lower end of the inner cylinder 255 in the one stage decomposition cylinder 47. In addition, the junction portion 500 is supplied with oil or vegetable oil or waste oil after their use in the tank 502, and a mixture of these oils and foam plastics is first and second decomposition in each tank. do. This makes it possible to recover the modified oil by a chemical decomposition reaction.

In general, as shown in FIG. 14, plastics such as polyethylene, polypropylene, polystyrene, ABS resin, acrylic resin, and the like are pyrolyzed to collect 90% as a product oil, and the other is employed as off gas (7 to 8%). It is processed by the off-gas treatment apparatus 34, and carbides (2 to 3%) are collected in the residue tank 40 as a residue. Polyvinyl chloride is neutralized by calcination, resulting in about 58% calcium chloride and about 42% pyrolysis, but about 30% is emulsified.

In addition, Japanese Patent Application No. 2002-017650 including the specification, the claims, the drawings and the summary filed on January 25, 2002, and the specification, the claims filed on October 16, 2002 All disclosures of Japanese patent application No. 2002-301895, including the scope, figures, and summaries, are incorporated herein by reference to all of them.

In addition, this invention is not limited to said embodiment. The said embodiment is an illustration, It has the structure substantially the same as the technical idea described in the claim of this invention, and what produces the same effect is contained in the technical scope of this invention.

As described above, the plastic emulsifying method and the emulsifying plant according to the present invention are useful as an emulsifying method and an emulsifying plant for collecting oil from waste plastic.

Claims (31)

A melting process of heating and dissolving the plastics to generate foamy plastics; Emulsifying method of plastic, characterized in that it comprises a decomposition step of taking out the foam-shaped plastic, heating, depolymerization and cooling to produce oil. The method of claim 1, The emulsification method of the plastic, characterized in that in the decomposition step to lift the bubble-shaped plastic up the slope upward. The method of claim 1, In the decomposition step, the plastic emulsifying method, characterized in that the bubble-shaped plastic is lifted out of the inclined upwards at an angle of 25 to 30 degrees with respect to the horizontal. The method of claim 2 or 3, In the decomposition step, the foamed plastics are heated while lifting upwards from the slope, and further, the foamed plastics are heated at a higher temperature as they are positioned upwards. The method of claim 1, In the dissolving step, the plastic is emulsified in a dissolving unit formed of a plurality of dissolving vessels having different temperature distributions. The method of claim 1, In the dissolving step, vegetable oil, animal oil or mineral oil is added to the dissolved plastic to produce a foam-shaped plastic composed of a mixture of the plastic and the vegetable oil, the animal oil or the mineral oil, In the decomposition step, the foamed plastics are emulsified, wherein the foamed plastics are taken out, heated, depolymerized and cooled to produce oil. The method of claim 1, In the decomposition step, the plastic is emulsified in the decomposition section formed by a plurality of decomposition cylinders having different temperature distribution and heated. The method of claim 1, And a hydrogen chloride gas treatment step of separating the hydrogen chloride gas generated when dissolving the plastic in the dissolving step from other decomposition gases and reacting with calcined lime to recover as calcium chloride. The method of claim 1, Emulsification method of the plastic, characterized in that further comprising an off-gas treatment step of contact decomposition of the off-gas not emulsified in the decomposition step with a high temperature ceramic. A melting part for heating and dissolving the plastic to produce a bubble-shaped plastic; Emulsifying plant characterized in that it comprises a decomposition unit for taking out the foam-shaped plastic, heating, depolymerization and cooling to produce oil. The method of claim 10, The disintegrating unit is an emulsification plant characterized in that it comprises a take-out means for lifting the bubble-shaped plastic up and out of the inclination. The method of claim 10, The disintegrating unit is an emulsification plant, characterized in that it comprises a take-out means for lifting the bubble-shaped plastic up the inclined upwards at an angle of 25 to 30 ° with respect to the horizontal. The method according to claim 11 or 12, The disintegrating unit is an emulsification plant, characterized in that it comprises heating means for heating the foam plastic in the upward direction of the inclination, and heating to a high temperature as the foam plastic is located above. The method of claim 10, The dissolution unit is an emulsification plant, characterized in that formed by a plurality of dissolution tanks having different temperature distribution. The method of claim 10, Emulsification plant characterized in that it comprises an oil injection means for injecting vegetable oil, animal oil or mineral oil at the junction of the dissolution unit and the decomposition unit. The method of claim 10, The decomposition unit is an emulsion plant, characterized in that formed by a plurality of inclined decomposition cylinder having a different temperature distribution. The method of claim 10, Further equipped with a dechlorination device for treating the hydrogen chloride gas generated in the melting portion, The dechlorination device is an emulsification plant, characterized in that formed with a separator for decomposing hydrogen chloride gas and other decomposition gas, and a reactor made of calcium chloride by reacting the hydrogen chloride gas decomposed by the separator with slaked lime. The method of claim 10, And an off-gas treating apparatus for contacting and decomposing off-gas not generated as oil after the cooling in the decomposing unit with a high-temperature ceramic. The method of claim 16, Emulsification plant, characterized in that the decomposition gas produced by depolymerization of the plastic in each of the decomposition cylinders provided in a multi-stage decomposition tank to cool the emulsion. The method of claim 16, Emulsion plant, characterized in that a super heater for further depolymerization of the plastic depolymerized in at least a portion of the decomposition tank. The method of claim 16, The decomposition vessel is an emulsified plant, characterized in that the heating temperature is gradually increased from below to upward. The method of claim 16, Emulsification plant characterized in that the residue recovery means provided on the upper end of the decomposition tank of the final stage of the decomposition tank provided in the multi-stage. The method of claim 22, And said residue recovery means is formed into a cylinder in which an upper opening is positioned at an upper end position of the decomposition tank of the final stage and the lower opening is positioned in an inert gas atmosphere that is heavier than air. The method of claim 10, A hopper for storing the plastic and supplying it to the dissolution unit; The hopper is an emulsion plant, characterized in that it comprises a lead screw having a spiral wing. The method of claim 24, Emulsion plant, characterized in that it further comprises a non-heating portion formed in the unheated region of a predetermined length between the hopper and the melting portion. The method of claim 14, The plurality of melt cylinders are provided with a lead screw having a spiral blade for conveying the plastic, Emulsion plant, characterized in that the pitch of the blade of the lead screw of the melting cylinder positioned at the beginning of the plurality of melting cylinders is larger than the pitch of the blade of the lead screw of the other melting cylinder. The method of claim 10, The melter and the decomposer are inner passages, outer cylinders formed on the outer periphery of the inner cylinders, hot air spaces through which hot air formed between the inner cylinders and the outer cylinders are circulated, and a temperature sensor for detecting a temperature of the dissolving portion or the decomposing portion. It is formed with a, And a carbon dioxide gas supply device for sending carbon dioxide gas to the hot air space when the temperature sensor detects an abnormal temperature that is equal to or higher than a predetermined temperature. The method of claim 10, The melting portion and the decomposition portion is formed with an inner cylinder, an outer cylinder formed on the outer periphery of the inner cylinder, and a hot air space through which hot air formed between the inner cylinder and the outer cylinder is circulated, A hot wind generator for generating hot wind for supplying the hot wind space by combustion; Further provided with a drying device for drying the plastic to be supplied to the melting furnace, Emulsification plant, characterized in that for supplying the air in the drying device to the hot air generating device to deodorize by combustion. The method of claim 18, Further provided with a drying device for drying the plastic to be supplied to the melting portion, Emulsifying plant, characterized in that for supplying the air in the drying apparatus to the off-gas treatment device by contact decomposition with a high temperature ceramic deodorizing. The method of claim 14, A part of the melter can be used to stretch and stretch the container, The telescopic cylinder is disposed in the inner cylinder, the outer periphery of the inner cylinder, one end is fixed to the inner cylinder and the other end is slid to the inner cylinder, and the other end of the bellows is fixed to the other end and the inner cylinder is slidable therein An oil painting plant, comprising: an outer cylinder housed therein. The method of claim 10, The melting portion is formed with an inner cylinder, an outer cylinder formed on the outer circumference of the inner cylinder, and a heat medium space formed between the inner cylinder and the outer cylinder and circulated with a liquid heat medium, Emulsion plant characterized in that it further comprises a heat medium supply device for supplying a heat medium of the liquid to the thermal catalyst space.