KR20210154503A - Recycling plant and method for producing recycled oil from waste synthetic resin - Google Patents

Abstract

The present invention relates to an emulsification apparatus and an emulsifying method for waste synthetic resin. The emulsification apparatus for waste synthetic resin comprises: a raw material supply part for supplying a raw material mixture in which the waste synthetic resin particles and a pore filler are mixed to a pyrolysis reactor; a pyrolysis reactor for generating organic gas by thermally decomposing the raw material mixture supplied from the raw material supply part; a cleaning tower for cleaning the organic gas generated in the pyrolysis reactor to generate cleaned organic gas and condensates; a condenser for condensing the organic gas cleaned in the cleaning tower to produce a condensate; a first separator for separating oil from the condensates generated in the cleaning tower; a second separator for separating oil from the condensate generated in the condenser; and a purification tower for producing regenerated oil by introducing the oil separated in the first separator and the second separator by fractional distillation. The present invention prevents the risk of explosion and increases the heat transfer efficiency in the thermal decomposition process of the waste synthetic resin, and produce high-purity regenerated oil from the waste synthetic resin in an efficient process.

Description

Emulsification apparatus and method for waste synthetic resin {RECYCLING PLANT AND METHOD FOR PRODUCING RECYCLED OIL FROM WASTE SYNTHETIC RESIN}

The present invention relates to an emulsification apparatus and an emulsification method for a waste synthetic resin, and according to one embodiment, it is possible to at least prevent the risk of explosion and increase the heat transfer efficiency in the thermal decomposition process of the waste synthetic resin. It relates to an emulsifying device and an emulsifying method for waste synthetic resin that can separate and produce recycled oil) in an efficient process.

Waste synthetic resins (waste plastic, waste vinyl, etc.) cause at least environmental problems if they are landfilled or incinerated. Waste synthetic resin does not decompose when it is landfilled and contaminates the soil. In addition, when the waste synthetic resin is incinerated, for example, SO _x , NO _x , HCl and dioxin are generated to cause air pollution.

Accordingly, various technologies for recycling waste synthetic resin have been proposed. A typical example is a chemical recycling technology using a thermal cracking process. Chemical recycling technology is to produce regenerated oil from waste synthetic resin, which is a technology that thermally decomposes waste synthetic resin to generate organic gas, and condenses (cools) the produced organic gas to convert it to fuel oil.

Chemical recycling technology uses an emulsifier with a pyrolysis reactor. In general, an emulsifying device for waste synthetic resin includes a pyrolysis reactor for thermally decomposing crushed waste synthetic resin through heating and melting under sealed conditions of high temperature/high pressure, a condenser for condensing (cooling) the organic gas generated in the pyrolysis reactor, and the condenser Includes a separator that separates and recovers the regenerated oil from the condensate (regenerated oil + moisture) generated in the

Although there are batch type batch type and screw type continuous type of emulsifier for waste synthetic resin, in most cases, continuous type is designed in consideration of productivity and energy efficiency. Such an emulsifying apparatus for waste synthetic resin is also presented in prior patent documents. For example, Korean Patent Laid-Open No. 10-2013-0081121, etc., propose a batch type emulsifying device, and Korean Patent No. 10-0945529, Korean Patent No. 10-1817728, and Korean Patent Publication No. A continuous type is proposed in 10-2010-0100366 and Korean Patent Laid-Open No. 10-2014-0093039, and the like.

However, the emulsification apparatus for waste synthetic resin and the emulsification method using the same according to the prior art, for example, have the following problems.

First, there is a risk of explosion in the pyrolysis process and the heat transfer efficiency is low. In general, in the thermal decomposition of the waste synthetic resin by heating and melting, the waste synthetic resin is crushed (crushed) into particles and then supplied to the pyrolysis reactor. At this time, voids are inevitably formed between the particles of the waste synthetic resin, and an air layer exists in the voids. When the waste synthetic resin particles accompanied by such an air layer are supplied to the pyrolysis reactor, the pyrolysis reactor may explode due to the expansion of the air layer due to high temperature/high pressure, which frequently occurred in the actual field. In addition, the heat transfer efficiency between the waste synthetic resin particles is lowered by the air layer, and accordingly, the amount of time and energy consumed for thermal decomposition is large.

In addition, in the conventional case, there is a problem in that waste synthetic resin is pyrolyzed and produced only by regenerated oil (fuel oil). In addition, the produced recycled oil is not subdivided into grades (gasoline grade, diesel grade, kerosene grade, etc.), and has low purity.

Korean Patent Publication No. 10-2013-0081121 Korean Patent Registration No. 10-0945529 Korean Patent Registration No. 10-1817728 Korean Patent Publication No. 10-2010-0100366 Korean Patent Publication No. 10-2014-0093039

Accordingly, an object of the present invention is to provide an improved emulsifying apparatus and emulsifying method.

According to one embodiment, the present invention can prevent at least the risk of explosion and increase heat transfer efficiency in the thermal decomposition process of the waste synthetic resin, and, together with the waste synthetic resin that can separate and produce high-purity regenerated oil from the waste synthetic resin in an efficient process An object of the present invention is to provide an emulsifying apparatus and an emulsifying method.

In order to achieve the above object, the present invention

a raw material supply unit for supplying a raw material mixture obtained by mixing the crushed waste synthetic resin particles and a pore filler filled in the voids between the waste synthetic resin particles to the pyrolysis reactor;

a pyrolysis reactor for generating organic gas by thermally decomposing the raw material mixture supplied from the raw material supply unit;

a cleaning tower for cleaning the organic gas generated in the pyrolysis reactor to generate cleaned organic gas and deposits;

a condenser for condensing the organic gas cleaned in the cleaning tower to produce a condensate;

a first separator for separating oil from deposits generated in the washing tower;

a second separator for separating oil from the condensate generated in the condenser; and

It provides an emulsifying apparatus for waste synthetic resin including a purification tower for introducing the oil separated in the first separator and the second separator and performing fractional distillation to produce regenerated oil.

In addition, the present invention,

A mixing process of obtaining a raw material mixture by mixing the crushed waste synthetic resin particles and a pore filler filled in the voids between the waste synthetic resin particles;

a pyrolysis process of thermally decomposing the raw material mixture to generate an organic gas;

a cleaning process of cleaning the organic gas generated in the pyrolysis process to generate cleaned organic gas and deposits;

a condensation process of condensing the organic gas cleaned in the cleaning process to generate a condensate;

a first separation process of separating oil from deposits generated in the washing process;

a second separation process of separating oil from the condensate generated in the condensation process; and

It provides a method for emulsifying a waste synthetic resin comprising a purification process of producing regenerated oil by fractionally distilling the oil separated in the first separation process and the second separation process.

In this case, the pore filler is a regenerated oil produced in the refining process, which includes a C1-C10 hydrocarbon-based compound.

According to the present invention, there is provided an improved emulsification apparatus and emulsification method capable of recycling waste synthetic resin as a useful resource.

According to the present invention, it has the effect of preventing the risk of explosion in the thermal decomposition process of the waste synthetic resin and increasing the heat transfer efficiency. Accordingly, it is possible to secure stability at least in the pyrolysis process and reduce the time and energy required for the pyrolysis process. In addition, according to the present invention, high-purity regenerated oil is separated and produced by grade from the waste synthetic resin, so that the reactivity of the waste synthetic resin is improved.

1 is a schematic configuration diagram showing an emulsifying apparatus for waste synthetic resin according to an embodiment of the present invention.
2 is a block diagram of a raw material supply unit constituting an emulsifying apparatus for waste synthetic resin according to an embodiment of the present invention.
3 is a block diagram of a pyrolysis reactor and a washing tower constituting an emulsification apparatus for waste synthetic resin according to an embodiment of the present invention.
4 is a block diagram of a condenser constituting an emulsifying apparatus for waste synthetic resin according to an embodiment of the present invention.
5 is a block diagram of a purification tower constituting an emulsifying apparatus for waste synthetic resin according to an embodiment of the present invention.
6 to 19 are views showing the heat supply means for transferring the sludge discharge unit constituting the emulsification apparatus of the waste synthetic resin according to an embodiment of the present invention.

The term "and/or" used in the present invention is used to mean including at least one or more of the components listed before and after. The terms "first", "second", "one side" and "other side" used in the present invention are used to distinguish one component from another component, and each component is defined by the terms it is not going to be

Hereinafter, the present invention will be described with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS The accompanying drawings illustrate exemplary embodiments of the present invention, which are provided merely to aid understanding of the present invention. In addition, in describing the present invention, detailed descriptions of related well-known general-purpose functions and/or configurations will be omitted.

1 is a schematic configuration diagram showing an emulsifying apparatus for waste synthetic resin according to an embodiment of the present invention. 2 is a block diagram of the raw material supply unit 10, FIG. 3 is a block diagram of the pyrolysis reactor 20 and the washing tower 30, FIG. 4 is a block diagram of the condenser 40, and FIG. 5 is a refining tower ( 70) is shown.

1 to 5, the waste synthetic resin emulsification apparatus according to the present invention is a raw material supply unit 10 for supplying a raw material mixture in which the waste synthetic resin particles and the pore filler are mixed to the pyrolysis reactor 20; a pyrolysis reactor 20 for generating organic gas by thermally decomposing the raw material mixture supplied from the raw material supply unit 10; a cleaning tower 30 for cleaning the organic gas generated in the pyrolysis reactor 20 to generate cleaned organic gas and deposits; a condenser 40 for condensing the organic gas washed in the washing tower 30 to generate a condensate; a first separator (61) for separating oil from the deposits generated in the washing tower (30); a second separator 62 for separating oil from the condensate generated in the condenser 40; and a purification tower 70 for producing regenerated oil by introducing the oil separated in the first and second separators 61 and 62 and performing fractional distillation.

In addition, the emulsification method of the waste synthetic resin according to the present invention is a mixing process of obtaining a raw material mixture by mixing the waste synthetic resin particles and the pore filler; a pyrolysis process of thermally decomposing the raw material mixture to generate an organic gas; a cleaning process of cleaning the organic gas generated in the pyrolysis process to generate cleaned organic gas and deposits; a condensation process of condensing the organic gas cleaned in the cleaning process to generate a condensate; a first separation process of separating oil from deposits generated in the washing process; a second separation process of separating oil from the condensate generated in the condensation process; and a refining process of fractionally distilling the oil separated in the first and second separation processes to produce regenerated oil.

According to one embodiment, the emulsification method of the waste synthetic resin according to the present invention includes a raw material supply process (mixing), a pyrolysis process, a washing process, a condensation process, a separation process, a purification process, a return process, and a sludge discharge process. Hereinafter, an emulsification apparatus for waste synthetic resin according to an embodiment of the present invention will be described while explaining a method for emulsifying waste synthetic resin according to an embodiment of the present invention with reference to the accompanying drawings.

[1] Raw Material Feed

In the present invention, the waste synthetic resin is waste plastic and waste vinyl, etc., which are not particularly limited. Waste synthetic resin is generated at industrial sites or general households, for example, polyethylene (PE), polypropylene (PP), polystyrene (PS), polyvinyl chloride (PVC), polyacrylic (PAc), polycarbonate (PC) , polyethylene terephthalate (PET) and/or vinyl-based materials may be included. These waste synthetic resins are washed and dried, crushed (or pulverized) to a predetermined size, and then used after being granulated.

The raw material supply unit 10 obtains a raw material mixture in which the crushed waste synthetic resin and the pore filler are mixed, and then supplies the raw material mixture to the pyrolysis reactor 20 . The waste synthetic resin may be supplied to the pyrolysis reactor 20 through the classification operation, for example, one of the above-listed types is used, or two or more types are mixed. According to one embodiment, the fuel supply unit 10 includes a crusher (or pulverizer) 13 for crushing (or pulverizing) of the waste synthetic resin, and a mixer 14 for mixing the crushed waste synthetic resin particles with the pore filler and , a pore filler supply line L10 for supplying the void filler to the mixer 14, and a feed pump for pumping the raw material mixture mixed in the mixer 14 and supplying it to the pyrolysis reactor 20 ( 15).

According to a more specific embodiment, the raw material supply unit 10 is a carrier means 12 such as a crane for transporting and injecting the waste synthetic resin transported through the transport means 11 such as a truck to the crusher 13. And, a crusher 13 that crushes (or pulverizes) the waste synthetic resin transferred and injected through the carrier means 12 to generate waste synthetic resin particles, and the waste synthetic resin particles and void filler injection line generated in the crusher 13 A mixer 14 for mixing the void filler supplied through (L10), a void filler supply line L10 for supplying the void filler to the mixer 14, and a raw material mixture mixed in the mixer 14 ( It may include a feed pump 15 for pumping a mixture of waste synthetic resin particles and pore filler) and supplying it to the pyrolysis reactor 20 .

The mixer 14 is not particularly limited as long as it can mix the waste synthetic resin particles and the pore filler. The mixer 14 may have a structure in which stirring means or vibration means are installed in some cases in order to improve the uniform mixing of the waste synthetic resin particles and the pore filler. In addition, the mixer 14 may have a closed structure, and may have a vent part for discharging internal air to the outside. The vent unit may be installed, for example, at an upper end of the mixer 14, and a check valve and/or an air permeable membrane may be installed in the vent unit.

A gap is formed between the waste synthetic resin particles introduced into the mixer 14 and the waste synthetic resin particles, and an air layer exists in these gaps. The pore filler is filled (filled) in the voids between the waste synthetic resin particles, thereby removing at least an air layer present in the voids.

According to one embodiment, when the void filler is supplied to the inside of the mixer 14 at a predetermined pressure through the void filler supply line L10, the air present in the void is discharged to the outside through the vent and removed, The pores are filled with a pore filler. By means of such a void filler, at least the risk of an explosion can be avoided (elimination). Specifically, when the waste synthetic resin particles accompanying the air layer are directly supplied to the pyrolysis reactor 20, the air layer expands by high temperature/high pressure and the pyrolysis reactor 20 may explode, but according to the embodiment of the present invention, the voids If the air layer is removed by means of the filler, at least the risk of explosion in the pyrolysis process is avoided (removed). In addition, as the air layer is removed, a non-oxidizing atmosphere (oxygen-free atmosphere) is formed inside the pyrolysis reactor 20 to prevent combustion and cocking, and increase carbonization efficiency. Here, carbonization means that the waste synthetic resin (organic material) is converted into a hydrocarbon compound having a high carbon content by thermal decomposition.

In addition, according to the present invention, heat transfer efficiency is improved by the pore filler, thereby reducing pyrolysis time and energy consumption in the pyrolysis process. Specifically, the pore filler acts as a heat transfer medium for transferring heat between the waste synthetic resin particles to improve thermal decomposition efficiency. Preferably, the pore filler may have a predetermined temperature. The pore filler, for example, may have a temperature of 50 ℃ or more, for example, 50 ℃ ~ 250 ℃. When the temperature of the pore filler is less than 50° C., heat transfer efficiency may be insignificant. And when the temperature of the pore filler is high by exceeding 250° C., for example, oil vapor is generated by melting of the waste synthetic resin, and the supply pump 15 is adversely affected by the oil vapor, or the supply pump 15 and pyrolysis There is a risk of leakage or damage due to high pressure in the raw material supply line (L15) installed between the reactors (20). In consideration of this point, the pore filler may have a temperature of 80°C or higher, for example, it may have a temperature of 80°C to 230°C.

According to a preferred embodiment, the pore filler may include a C1-C10 hydrocarbon-based compound. Here, the C1-C10 hydrocarbon-based compound is a hydrocarbon-based compound having 1 to 10 carbon atoms in the molecule, and includes C1-C10 alkane-based compounds, alkene-based compounds, and derivatives (substituents) thereof. The C1 to C10 hydrocarbon-based compound may include, for example, methane, ethane, propane, butane, pentane, hexane, heptane, octane, nonane, tecan and/or derivatives (substituents) thereof, and the like. When using the above C1-C10 hydrocarbon-based compound as a pore filler, the spreadability is higher than when using a viscous material, so the pore filling efficiency (air layer removal ability) is improved. Energy consumption for its own phase change can be reduced.

The C1 to C10 hydrocarbon-based compound may be supplied to the mixer 14 at a pressure of 2 atm to 5 atm and a temperature of 80° C. to 230° C. in consideration of pore filling efficiency and heat transfer efficiency. have. When the C1 to C10 hydrocarbon-based compound has a pressure and temperature within the above range, pore filling efficiency and heat transfer efficiency are improved, and there is a risk of leakage or damage in the process of being transferred to the pyrolysis reactor 20 together. can These C1-C10 hydrocarbon-based compounds may be supplied to the mixer 14 in a gaseous, liquid, or gas-liquid mixed phase through the pore filler supply line L10. At this time, the liquid phase may be different depending on the type of the hydrocarbon-based compound, for example, hydrocarbon-based compounds such as C1 to C5 may be supplied in the liquid phase through compression.

According to a preferred embodiment, the pore filler may be used by returning light high-grade oil (gasoline grade, etc.) separated from the rectification tower 70 . Such light feed oil has C1 ~ C10 hydrocarbon-based compounds as a main component. This will be described later.

In the mixer 14, 0.5 to 40 parts by weight, 2 to 35 parts by weight, 5 to 35 parts by weight, or 10 to 30 parts by weight of the pore filler may be supplied and mixed with respect to 100 parts by weight of the waste synthetic resin particles, but limited by this it is not going to be For another example, in the mixing in the mixer 14, 10 pore fillers are added based on the total weight of the raw material mixture according to the type of waste synthetic resin particles, the type of pore filler, the type of desired product and/or the desired product production volume, etc. ~ 20% by weight, 20 ~ 30% by weight or 30 ~ 40% by weight can be used.

The feed pump 15 may pump the raw material mixture mixed in the mixer 14 to supply the pyrolysis reactor 20 . The supply pump 15 may be selected from a suction pump capable of blocking leakage or inflow of air. The supply pump 15 is used for pumping mortar or concentrated sludge in general industry, and an interflex pump having strong suction and discharge power can be usefully used.

In addition, the fuel supply unit 10 includes the mixer 14, the supply pump 15 and the pore filler supply line L10 as described above as one set, and includes one or two or more of these sets. can In the drawing, the mixer 14, the feed pump 15, and the void filler supply line L10 are each installed as three sets.

[2] Thermal cracking

The raw material mixture is supplied to the pyrolysis reactor 20 along the raw material supply line L15 by pumping the feed pump 15 . The pyrolysis reactor 20 pyrolyzes waste synthetic resin through a high-temperature/high-pressure pyrolysis process (heat melting) to generate organic gas, which is the same as usual. One, two or more of these pyrolysis reactors 20 may be installed in plurality in the emulsification apparatus according to the present invention, and in the case of installing a plurality of them, they may be connected in parallel and/or in series. The pyrolysis reactor 20, for example, is maintained at a temperature of 350 ° C. to 650 ° C., for example, a temperature of 450 ° C. to 600 ° C. and a pressure of 3 atmospheres (atm) to 7 atmospheres, from the waste synthetic resin to organic gas can create

According to a preferred embodiment, the pyrolysis reactor 20 may be heated by high-frequency induction heating. In the case of using high-frequency induction heat, thermal decomposition efficiency may be improved by at least a fast heating rate. In addition, a preheater (not shown) may be installed in the raw material supply line L15 installed between the pyrolysis reactor 20 and the supply pump 15 . The raw material mixture supplied to the pyrolysis reactor 20 is preferably maintained at a temperature of about 200° C. to 250° C. by the preheater, and more specifically, maintained at a temperature of 210° C. to 230° C. When the raw material mixture is supplied to the pyrolysis reactor 20 by maintaining a temperature of 200° C. to 250° C., it is advantageous in thermal decomposition efficiency and energy reduction. When the raw material mixture supplied to the pyrolysis reactor 20 is, for example, less than 200° C., the energy consumption for temperature increase in the pyrolysis reactor 20 may be high and the pyrolysis rate may be low. And when the raw material mixture supplied to the pyrolysis reactor 20 exceeds, for example, 250° C., although a small amount, organic gas is generated before flowing into the pyrolysis reactor 20 through the raw material supply line L15, so that the raw material supply line (L15) or the pyrolysis reactor 20, there is a risk of leakage or damage due to high pressure.

A first flow line L11 is installed between the pyrolysis reactor 20 and the cleaning tower 30 . The first flow line L11 connects the pyrolysis reactor 20 and the cleaning tower 30 to supply the organic gas generated in the pyrolysis reactor 20 to the cleaning tower 30 . That is, the organic gas generated in the pyrolysis reactor 20 is supplied to the cleaning tower 30 along the first flow line L11. The first flow line L11 may connect the upper end of the pyrolysis reactor 20 and the upper end of the cleaning tower 30 to provide a flow path for the organic gas. At this time, a heater 25 for maintaining the organic gas supplied to the cleaning tower 30 at 200° C. to 250° C. may be installed in the first flow line L11. The heater 25 may maintain the organic gas at a temperature in an appropriate range (200° C. to 250° C.) through high-frequency induction heat.

In addition, a sludge discharge line (L22) is connected to the lower end of the pyrolysis reactor (20). The sludge generated in the pyrolysis reactor 20 is supplied to the sludge discharge unit 90 along the sludge discharge line L22.

[3] Cleaning

The organic gas generated in the pyrolysis reactor 20 is supplied to the cleaning tower 30 along the first flow line L11. The cleaning tower 30 is for cleaning (purifying) the organic gas, which includes, for example, low-density organic gas (higher fraction of light oil) and high-density heavy fraction (lower fraction of heavy oil) contained in organic gas. separate One, two or more of these washing towers 30 may be installed in plurality in the emulsifying apparatus according to the present invention, and when a plurality of washing towers 30 are installed, they may be connected in parallel and/or in series.

The cleaning tower 30 may include, for example, a cyclone 32 . The cleaning tower 30 includes a cyclone 32 installed at an inner lower end thereof, and may further include a steam injector 34 in addition to this. The steam sprayer 34 may spray high-temperature/high-pressure steam from the upper end of the cleaning tower 30 . The steam injector 34 may inject steam having a temperature of 150 to 200° C. under a high pressure condition in order to prevent condensation of the organic gas. At this time, the sediment (sediment) containing at least a high-density heavy powder, etc. is separated downward by the cyclone 32, and at least a steam-friendly material (e.g., nitride, sulfide, water-soluble substances such as carbonate), etc. may be adsorbed, separated and washed.

A second flow line L12 is installed between the washing tower 30 and the condenser 40 . The second flow line L12 connects the cleaning tower 30 and the condenser 40 to supply the organic gas cleaned in the cleaning tower 30 to the condenser 40 . That is, the organic gas cleaned in the cleaning tower 30 is discharged to the side of the cleaning tower 30 and supplied to the condenser 40 along the second flow line L12. At this time, one side of the second flow line (L12) may be connected to the approximately middle side of the cleaning tower (30). More specifically, one side of the second flow line L12 is located between the cyclone 32 and the steam injector 34 , and may be connected to the steam injector 34 in close proximity. The other side of the second flow line L12 may be connected to the upper end of the condenser 40 to supply the cleaned organic gas downward to the condenser 40 .

In addition, a first oil recovery line L31 is connected to the lower end of the washing tower 30 . The high-density heavy powder (and steam-friendly material) separated in the washing tower 30 is supplied to the first separator 61 along the first oil recovery line L31. In this case, the pump P may be installed in the first oil return line L31 connecting the lower end of the washing tower 30 and the first separator 61 . The pump P is for pumping the high-density heavy powder separated to the lower end of the washing tower 30 and supplying it to the first separator 61, which is, for example, an interflex pump as described above. can be used

Therefore, in the washing tower 30, the organic gas supplied from the pyrolysis reactor 20 is washed (purified) to generate a high-purity organic gas (high-grade fraction), and the high-density heavy fraction is removed from the cyclone 32, etc. It separates downward in the form of sediment through At this time, the deposit is supplied to the first separator 61, and the high-purity organic gas is supplied to the condenser 40 along the second flow line L12.

The cleaning in the cleaning tower 30 is preferably performed by introducing the organic gas generated in the thermal decomposition process at 200°C to 250°C. Specifically, as described above, the organic gas generated in the pyrolysis reactor 20 is supplied to the cleaning tower 30 through the heater 25, for example, while maintaining a temperature of 200° C. to 250° C. It's good, but it has the following technical significance.

When the temperature of the organic gas flowing into the cleaning tower 30 is low, for example, less than 200° C., although a small amount, it is condensed in the cleaning tower 30 or floated in the cleaning tower 30 The density (the amount of the floating organic gas) is lowered so that the discharge amount discharged along the second flow line L12 becomes smaller. Accordingly, the amount of high-purity organic gas supplied to the condenser 40 is reduced, and consequently, the production rate of high-purity regenerated oil is reduced. In addition, when the temperature of the organic gas exceeds 250° C. and is too high, there is a risk of water leakage or damage in the flow lines L11 ( L12 ), the device connection portion, and the like.

[4] Condensation

The high-purity organic gas washed in the washing tower 30 is supplied to the condenser 40 to be condensed (cooled). The condenser 40 condenses the high-purity organic gas introduced along the second flow line L12 to generate a liquid condensed condensate (containing a large amount of oil). A second oil return line L32 is connected to the lower end of the condenser 40 . The condensate generated in the condenser 40 is supplied to the second separator 62 along the second oil recovery line L32. One or two or more of these condensers 40 may be installed in a plurality in the emulsification apparatus according to the present invention, and when a plurality of condensers 40 are installed, they may be connected in parallel and/or in series.

In addition, a third flow line L13 through which a portion of the organic gas introduced into the condenser 40 is discharged is installed on the side of the condenser 40 . The third flow line L13 is connected to the side of the condenser 40 to discharge non-condensed organic gas that is not condensed in the condenser 40 . One side of the third flow line L13 may be connected to the side of the condenser 40 , and the other side of the third flow line L13 may be connected to the regenerated oil storage tank T13 . At this time, the organic gas discharged through the third flow line (L13) is of high purity, and it also contains a large amount of low-molecular-weight hydrocarbon-based compounds and can be used as high-grade oil.

According to the present invention, as a result of analyzing the organic gas introduced into the condenser 40, it was found that a large amount of a low molecular weight hydrocarbon-based compound was contained. In addition, according to the present invention, as a result of performing the condensation process in a state in which the third flow line L13 is connected to the side of the condenser 40, most of the organic gas containing the oil component is condensed and discharged to the lower side to be condensed It was found that separated into water (containing a large amount of oil), some organic gas was not condensed and discharged as non-condensed organic gas along the third flow line L13. At this time, it was found that the non-condensed organic gas is a high-purity and high-grade oil, which contains a large amount of a C1-C10 hydrocarbon-based compound having a very high octane number.

Therefore, the condenser 40 condenses most of the organic gas among the high-purity organic gas introduced from the washing tower 30 to generate a condensate (containing a large amount of oil) for the production of regenerated oil, along with some non-condensing Separate the organic gas. That is, according to the embodiment of the present invention, in the condensation process, the organic gas cleaned in the cleaning process is introduced into the condenser 40 , and then a condensed (cooled) condensate is generated, and the condensate is Discharge to the bottom and separate. At the same time, the non-condensed organic gas that is not condensed in the condenser 40 is generated and separated to the side of the condenser 40 .

The non-condensed organic gas may be recovered and stored in a separate regenerated oil storage tank T13. Such non-condensed organic gas contains a large amount of high-purity and low-molecular-weight hydrocarbon-based compounds, for example, C1-C4 hydrocarbon-based compounds (methane and ethane, etc.). The non-condensed organic gas is liquefied after being recovered to the regenerated oil storage tank T13, and may be used, for example, as high-purity high-grade fuel oil. As another example, the non-condensed organic gas may be used as a raw material for production of hydrogen. Non-condensed organic gas contains a large amount of C1-C4 hydrocarbon-based compounds (methane and ethane, etc.), and these C1-C4 hydrocarbon-based compounds (methane and ethane, etc.) can be switched _{As an example, methane (CH 4} ) contained in the non-condensed organic gas may be converted into hydrogen through high-temperature pyrolysis reforming at 500° C. or higher.

In addition, according to the embodiment of the present invention, in the condensation process, the organic gas cleaned in the cleaning process is maintained at a temperature of about 150° C. or higher, introduced into the condenser 40, and the pressure of the condenser 40 is about 10 kg/cm 2 It is better to keep it above and proceed. Specifically, in the condensing process, the organic gas flowing into the condenser 40 along the second flow line L12 is maintained at a temperature of about 150° C. or higher, and the pressure in the condenser 40 is about 10 kg/cm 2 or higher. It is good to proceed with the separation of the non-condensed organic gas together with the condensation by maintaining it so that it becomes this. When the condensation process is performed under these process conditions, the output of the non-condensed organic gas, that is, the amount of the non-condensed organic gas that is discharged and separated through the third flow line L13 may be increased, which eventually results in a high-purity It is possible to increase the productivity of advanced fuel oil and/or hydrogen.

According to a specific embodiment, the inflow temperature of the organic gas flowing into the condenser 40 is maintained at 150° C. to 250° C., and the pressure in the condenser 40 is maintained at 10-25 kg/cm 2 to proceed with the condensation process. can When the inlet temperature of the organic gas is less than 150° C. or the pressure in the condenser 40 is less than 10 kg/cm 2 , the amount of the non-condensed organic gas discharged and separated through the third flow line L13 may be lowered. In addition, when the inflow temperature of the organic gas exceeds 250° C. or the pressure in the condenser 40 exceeds 25 kg/cm 2 , the condensation efficiency is lowered, for example, the condensate separated to the lower end of the condenser 40 Production (production of oil) may be lowered. In consideration of this, it is preferable to perform the condensation process under temperature/pressure conditions in which the inflow temperature of the organic gas is maintained at 180° C. to 230° C., and the pressure in the condenser 40 is maintained at 12 to 20 kg/cm 2 . do.

At this time, the inflow temperature of the organic gas introduced into the condenser 40 is, for example, a temperature of about 150° C. or higher, specifically 150° C., through a preheater (not shown) installed on the second flow line L12. ~ 250 ℃ temperature (preferably 180 ℃ ~ 230 ℃ temperature) can be adjusted to be maintained. In addition, the pressure in the condenser 40 is a pressure of about 10 kg/cm 2 or more, specifically, a pressure of 10 to 25 kg/cm 2 (preferably 12 to 20 kg / cm2).

In addition, in the condensing process, for example, by proceeding under the above temperature and pressure conditions, the ratio of the discharge flow rate of the non-condensed organic gas to the flow rate of the organic gas flowing into the condenser 40 is 3% or more. can That is, the discharge ratio (R) of the non-condensed organic gas according to the following Equation 1 may be 3% or more, specifically 3 to 15%, or 5 to 12%. In the case of having such a discharge ratio (R), the production of non-condensed organic gas, that is, the production (discharge) of high-purity high-grade fuel oil produced (discharged) along the third flow line (L13) and the production of condensate, that is, the condenser ( 40), both of the production volumes of oil (regenerated oil) finally produced by being separated at the lower end can be appropriately optimized.

[Equation 1]

R(%) = (Q _out / Q _in ) x 100

In Equation 1, R is the discharge ratio of the non-condensed organic gas, Q _out is the discharge flow rate of the non-condensed organic gas discharged and separated through the third flow line (L13). And Q _in is the inflow flow rate of the organic gas introduced into the condenser 40, which is specifically the inflow of the organic gas flowing into the condenser 40 through the second flow line L12 from the cleaning tower 30 is the flow

[Table 1] below shows the output ratio (R) of the non-condensed organic gas according to the production amount of the non-condensed organic gas, that is, the inlet temperature (T _in ) and the pressure (P _{g ) according to an embodiment of the present invention.} As shown in Table 1 below, the inflow temperature (T _in ) of the organic gas introduced into the condenser 40 and the pressure (P _g ) in the condenser 40 were varied according to each embodiment. As the organic gas introduced into the condenser 40, an organic gas of a waste synthetic resin containing polyethylene (PE) as a main component was used, and the discharge ratio (R) was calculated according to Equation 1 above.

< Production of non-condensed organic gas according to the conditions of the condensation process > note T _in P _g R(%) Example 1 86℃ 8.1kg/cm2 - Example 2 128℃ 7.2kg/cm2 - Example 3 152℃ 8.7kg/cm2 0.76 Example 4 154℃ 10.6kg/cm2 3.12 Example 5 184℃ 12.4kg/cm2 5.08
* T _in : Inlet temperature (℃) of organic gas flowing into the condenser
* P _g : Pressure in the condenser (kg/cm2)
* R(%) : Ratio (percentage) of the outlet flow rate (Q _{out ) to the inlet flow rate (Q in )}

As shown in [Table 1], the discharge rate (R) of the non-condensed organic gas according to _{the inlet temperature (T in} ) of the organic gas flowing into the condenser 40 and the pressure (P _{g ) in the condenser 40} , that is, it was found that the emission of non-condensed organic gas was different. As in Examples 1 and 2, when the inlet temperature (T _in ) and the pressure (P _g ) were too low, it was found that almost no emission of non-condensed organic gas occurred, and Examples 4 and Example 4 As in 5, when the inlet temperature (T _in ) and the pressure (P _g ) were 150° C. or more and 10 kg/cm 2 or more, respectively, it was found that good discharge (discharge rate of 3% or more) was shown.

[5] Separation

The first separator 61 separates oil (regenerated oil) from the sediment (containing high-density heavy content, etc.) introduced through the first oil recovery line L31. In addition, the second separator 62 separates high-purity oil (regenerated oil) from the condensate (containing high-purity oil) introduced through the second oil recovery line L32. As long as the first and second separators 61 and 62 can separate oil (regenerated oil) from each influent, it may include, for example, an oil-water separator. One or two or more of these first and second separators 61 and 62 may be installed in the emulsifying apparatus according to the present invention, and in the case of installing a plurality of them, they may be connected in parallel and/or in series.

The regenerated oil separated by the first and second separators 61 and 62 is supplied to the purification tower 70 along the fourth flow line L14. In addition, in the first and second separators 61 and 62, a residue remaining after separating the reclaimed oil is generated, and the residue contains a large amount of moisture and the like. After these residues are discharged along the wastewater line L23, they may be transported to a separate treatment plant (eg, a wastewater treatment plant) for treatment.

[6] Refining

The oil (regenerated oil) separated by the first and second separators 61 and 62 is supplied to the refining tower 70 along the fourth flow line L14 for purification. At this time, the refining tower 70 introduces oil (regenerated oil) and separates it according to the boiling point, thereby producing (refining) high-purity regenerated oil for each grade. One or two or more of these refining towers 70 may be installed in plurality in the emulsifying apparatus according to the present invention, and when a plurality of refining towers 70 are installed, they may be connected in parallel and/or in series.

The purification tower 70 includes a fractionation column 72 for fractionally distilling the oil introduced from the first separator 61 and the second separator 62, and the regenerated oil separated in the fractionation column 72 is recovered by grade. It may include a reclaimed oil return line (L70). The purification tower 70 may include a multi-stage distillation stage 74 installed in the fractionation column 72 , and may separate the regenerated oil according to the boiling point in each distillation stage 74 of the fractionation column 72 by grade. Refining tower 70, for example, petroleum gas grade (such as methane and ethane), gasoline grade (naphtha), diesel grade, kerosene grade, such as renewable oil can be separated by grade.

The regenerated oil separated in the refining tower 70 is discharged to the regenerated oil recovery line L70 connected to the side of the fractionation tower 72 , and then is supplied to the regenerated oil recovery tank 80 to be recovered and stored. That is, one side of the regenerated oil recovery line L70 is connected to the side of the fractionation column 72 , and the other side of the regenerated oil recovery line L70 is connected to the regenerated oil recovery tank 80 . In this case, the regenerated oil recovery line L70 may be installed in plurality so that the regenerated oil separated in the refining tower 70 can be recovered by grade. Specifically, a plurality of regenerated oil recovery lines L70 corresponding to the number of grades of regenerated oil may be connected to the side of the fractionation column 72 . The regenerated oil recovery line (L70) is, for example, a petroleum gas class regenerated oil recovery line (L71), a gasoline class (naphtha) regenerated oil recovery line (L72), a diesel class regenerated oil recovery line so that the regenerated oil can be recovered by grade. It may include a line L73, a kerosene-grade regenerated oil recovery line L74 and a bunker oil recovery line L75, and the like.

In the case of the regenerated oil recovery tank 80, a plurality of regenerated oil may be recovered and stored by grade, which may include, for example, a petroleum gas-grade regenerated oil recovery tank, a gasoline-grade (naphtha) regenerated oil recovery tank, It may include a diesel-grade recycled oil recovery tank, a kerosene-grade recycled oil recovery tank, and a bunker oil recovery tank.

In addition, the regenerated oil may be liquefied and stored in the regenerated oil recovery tank 80 . For example, a liquefier (not shown) is installed in the regenerated oil recovery line (L70) or a liquefier (not shown) is installed in the regenerated oil recovery tank 80, and is separated from the purification tower (70) The regenerated oil may be liquefied and stored in the regenerated oil recovery tank 80 . The regenerated oil stored in the regenerated oil recovery tank 80 has a high purity, which may be recycled, for example, as fuel oil.

In addition, a low fuel oil discharge line L24 may be connected to the lower end of the refining tower 70 . The low fuel oil generated in the refining tower 70 is discharged to the low fuel oil discharge line L24. The low oil supply may be supplied to the sludge discharge unit 90 along the low oil supply discharge line L24 by the suction force of the pump P to be treated. In some cases, the low fuel oil generated in the refining tower 70 may be supplied to the raw material supply unit 10 and reprocessed through processes such as pyrolysis, washing, condensation and fractional distillation. In this case, the low fuel oil discharge line L24 may be connected to the mixer 14 of the raw material supply unit 10 so that the low fuel oil discharged to the lower end of the refining tower 70 can be supplied to the raw material supply unit 10 .

[7] Return

As mentioned above, the pore filler supplied to the mixer 14 may be used by returning the regenerated oil (light high-grade oil) produced and separated in the rectification tower 70 . As described above, in the rectification tower 70, regenerated oil such as petroleum gas grade (methane and ethane, etc.), gasoline grade (naphtha), diesel grade and kerosene grade is separated by grade through fractional distillation. At this time, petroleum gas grade and / Or gasoline-grade regenerated oil may be returned (supplied) to the mixer 14 and used as a pore filler. Such petroleum gas and/or gasoline-grade regenerated oil contains a hydrocarbon-based compound having a high octane number of C1 to C10, and thus may be usefully used as the pore filler.

To this end, among the plurality of recycled oil recovery lines (L70), a petroleum gas grade recycled oil recovery line (L71) and/or a gasoline grade recycled oil recovery line (L72) may be connected to the pore filler supply line (L10). . For another example, among the plurality of regenerated oil recovery tanks 80, a petroleum gas regenerated oil recovery tank and/or a gasoline regenerated oil recovery tank is connected to the void filler supply line L10, and the mixer 14 As a pore filler, petroleum gas grade and/or gasoline grade regenerated oil having a high octane number can be supplied.

[8] Sludge Discharge

The sludge generated in the pyrolysis reactor 20 is supplied to the sludge discharge unit 90 along the sludge discharge line L22. In addition, as mentioned above, the low fuel oil generated in the refining tower 70 may be supplied to the sludge discharge unit 90 along the low fuel oil discharge line L24.

The sludge discharge unit 90 may collect and temporarily store the sludge generated in the pyrolysis reactor 20 and/or the low fuel oil generated in the purification tower 70 . The sludge discharge unit 90 is, for example, a sludge hopper 92 into which sludge (and/or regenerated oil) flows, and a transfer heat supply means installed at the lower end of the sludge hopper 92 to apply heat while transferring the sludge. (94), and may include a storage unit (not shown) for collecting and storing the sludge that has passed through the transfer heat supply means (94). The sludge collected in the sludge discharge unit 90 may be transferred to a production facility such as Char or Carbon for treatment.

In the present invention, each of the lines L10 to L32 is not particularly limited as long as it can provide a flow path through which a raw material or gas can pass. Each of the lines L10 to L32, for example, may be made of a material selected from a metal material, a synthetic resin material, and/or a ceramic material, and includes a hard and/or flexible material. In addition, a valve, a pump, a pressure gauge, a flow meter, a thermometer, a liquid level gauge and/or a controller, etc. may be installed in each of the lines L10 to L32 and each component of the device, and the valve operates to open/close and/or control the flow rate This may be possible.

According to the present invention described above, it is possible to at least prevent the risk of explosion in the thermal decomposition process of the waste synthetic resin and increase the heat transfer efficiency. Accordingly, in reusing the waste synthetic resin as a useful resource by emulsifying it, it is possible to secure the safety of the process and reduce the time and energy required for the pyrolysis process. In addition, according to the present invention, it is possible to produce high-purity regenerated oil for each grade from the waste synthetic resin, and it is possible to improve the production speed and the like. In addition, the non-condensed organic gas discharged and separated from the condenser 40 into the third flow line L13 is a high-purity and low-molecular-weight hydrocarbon-based compound (methane, ethane, etc.) milk can be produced.

On the other hand, the transfer heat supply means 94 of the sludge discharge unit 90 may be configured as follows. This will be described with reference to FIGS. 6 to 19 . 6 is a block diagram of a main part of the transfer heat supply means 94 according to the embodiment of the present invention, and FIGS. 7 and 8 are cross roller bearings constituting the transfer heat supply means 94 according to the embodiment of the present invention. It is a configuration diagram. And Figs. 9 to 12 are block diagrams showing a retainer of a cross roller bearing constituting the transfer heat supply means 94 according to an embodiment of the present invention, and Figs. 13 to 19 are transfer heat supply according to an embodiment of the present invention. It is a block diagram which shows the absorption part which comprises the means 94. As shown in FIG.

First, referring to Figure 6, the transfer heat supply means 94 is a shaft (SH) rotated by a drive motor (M), a screw (SW) formed on the outer periphery of the screw (SW) to transfer the sludge, It may include a driving motor M for rotating the shaft SH, and a heat supplier for applying heat to the sludge transferred by the screw SW. At this time, the heat supplier may apply, for example, high-frequency induction heat to the sludge.

The shaft SH is supported by a case CA, and a cross roller bearing CR is provided between the shaft SH and the case CA. The crossed roller bearing CR is a bearing in which the rollers CR1 are crossed in a direction perpendicular to each other as shown in FIGS. 7 and 8 . These crossed roller bearings can withstand loads in various directions and are advantageous in rigidity, precision and durability compared to their small size. The sludge treated in the sludge discharge unit 90 has high viscosity and high viscosity (sticky), which may apply a force (pressure) to the drive shaft SH in various directions. Accordingly, it is preferable that the bearing supporting the drive shaft SH rotatably also use the cross roller bearing.

The crossed roller bearing CR includes a retainer 400 as shown in FIG. 8 . The retainer 400 is disposed between the rollers CR1 and a through hole (not shown) is formed on one side of the retainer 400 to allow the grease to flow.

According to an embodiment of the present invention, the crossed roller bearing CR includes a retainer 400 disposed between a plurality of rollers CR4 as shown in FIGS. 9 to 13, wherein the retainer 400 includes a plate-shaped first retainer body 410 and a second retainer body 420 coupled to each other. The first retainer body 410 and the second retainer body 420 may be coupled to each other by bolts or the like, or may be coupled to each other by an adhesive or the like. In addition, the first retainer body 410 and the second retainer body 420 may have sides facing each other to be flat, and opposite sides may be formed to protrude with a specific curvature as shown.

At this time, according to the embodiment of the present invention, the first retainer body 410 and the second retainer body 420 are provided with a plurality of flow holes in addition to the conventionally used through holes TH, and a buffer part 500 to be described later is provided. provided In this case, the grease flows through the through hole of the retainer. If a high pressure is momentarily applied to the grease due to an external impact or the like, there is a fear that the above-described through hole may not guarantee the flow of the grease. In order to dispel these concerns, the configuration described below is adopted and described in detail.

As shown in FIG. 11 , a through hole TH on the side opposite to the second retainer body 420 of the first retainer body 410 of the present invention (left side in the drawing) and a lower side of the through hole TH A first central inlet hole 413 and a first side inlet hole 414 are formed in the . The first central inlet hole 413 is formed at a central point in the width direction as the lower side of the first retainer body 410 . A plurality of the first side inlet holes 414 are provided on both sides of the first central inlet hole 413 in the width direction. In the case of the illustrated embodiment, the first side inlet hole 414 is disposed one by one in the vertical direction on both sides of the first central inlet hole 413 to form a total of four.

In addition, as shown in FIG. 10 , a first upper seating groove 411 recessed in the thickness direction on the side of the first retainer body 410 in the direction (right side in the drawing) of the second retainer body 420 and the second retainer body 420 1 The lower seating grooves 412 are formed to be spaced apart in the height direction. At this time, the through-holes TH are formed on the left and right sides of the first upper seating groove 411 and the first lower seating groove 412 , respectively.

A first central communication hole 413 - 1 is formed below the first lower seating groove 412 to communicate with the first central inlet hole 413 . In addition, first side communication holes 414 - 1 are formed on both sides of the first central communication hole 413 - 1 in the width direction to communicate with the first side inlet hole 414 . At this time, a flow path FL is formed between the first central communication hole 413-1 and the first lower seating groove 412, and the first side communication hole 414-1 and the first lower seating groove A flow path FL is formed between the 412 . The flow path FL may be formed as a path having a relatively narrow width as shown. The first central communication hole 413-1 and the first lower seating groove 412 are communicated with each other by the flow path FL, and the first side communication hole 414-1 and the first lower seating groove ( 412) is communicated.

A first central storage groove 451-1 is recessed on the upper side of the first upper seating groove 411, and first side storage grooves 416- on both sides of the first upper seating groove 411 in the width direction. 1) is recessed, and a third storage groove 417 is recessed between the first upper seating groove 411 and the first lower seating groove 412, and the first central storage groove 451- A flow path FL is formed between 1), the first side storage groove 416-1, and the third storage groove 417 and the first upper seating groove 411, which will be described separately.

On the other hand, as shown in FIG. 10 , a through hole TH on the side (right side) opposite to the first retainer body 410 of the second retainer body 420 and a through hole TH on the upper side of the through hole TH The second central inlet hole 423 and the second side inlet hole 414 are formed. In addition, a third inlet hole 425 is formed between the through hole TH. The second central inlet hole 423 is formed at a central point in the width direction as the upper side of the second retainer body 420 , and the second side inlet hole 424 is the width direction of the second central inlet hole 423 . There are several on the side. That is, the second central inlet hole 423 and the second side inlet hole 424 are vertically symmetrical to the first central inlet hole 413 and the first side inlet hole 414 .

As shown in FIG. 11 , a second upper seating groove 421 and a second lower seating groove 422 recessed in the thickness direction on the side of the second retainer body 420 in the direction of the first retainer body 410 . It is formed spaced apart in this height direction. A second central communication hole 423-1 is formed on the upper side of the second upper seating groove 421 to communicate with the second central inlet hole 423, and the second central communication hole 423-1 Second side communication holes 424 - 1 are formed on both sides in the width direction to communicate with the second side inlet holes 424 . A flow path FL is formed between the second central communication hole 423-1 and the second lower seating groove 412, and the second side communication hole 424-1 and the second upper seating groove 421 are formed. ), a flow path FL is formed between them to communicate with each other.

On the other hand, a third communication hole 427 is formed on the upper side of the second lower seating groove 422 , and second side storage grooves 426 - 1 are formed on both sides of the second lower seating groove 422 in the width direction. The second central storage groove 425-1 is formed on the lower side of the second lower seating groove 422, and the second central storage groove 452-1 and the second side storage groove 426 are formed by being recessed. -1) and a flow path FL is formed between the third communication hole 427 and the second lower seating groove 422 .

That is, in the side surfaces of the first retainer 410 and the second retainer 420 facing each other, a first upper seating groove 411, a second upper seating groove 421, and a first lower seating groove ( 412) and the second lower seating groove 422 are respectively formed, and each communication hole is also formed in the same way. However, the difference is that only the third communication hole 427 is formed in the second retainer 420 .

On the other hand, the first side communication hole 414 - 1 and the first central communication hole 413 - 1 of the first retainer body 410 are formed in the second side storage groove 426 - 1 of the second retainer 420 and Each communicates with the second central storage groove 425-1, but the first side communication hole 414-1 and the first central communication hole 412-1 pass through the first retainer body 410 to allow the first It communicates with the side inlet hole 414 and the first central inlet hole 413 . However, the second side storage groove 426 - 1 and the second central storage groove 425 - 1 of the second retainer 420 are only formed to be concave and do not penetrate.

In addition, the second side communication hole 424 - 1 and the second central communication hole 423 - 1 of the second retainer body 420 are formed in the first side storage groove 416 - 1 of the first retainer 410 . and the first central storage groove 415-1, respectively, but the second side communication hole 424-1 and the second central communication hole 422-1 pass through the second retainer body 420 and It communicates with the second side inlet hole 424 and the second central inlet hole 423 . However, the first side storage groove 416 - 1 and the first central storage groove 415 - 1 of the first retainer 410 are only formed to be concave and do not penetrate.

Hereinafter, a process in which the grease flows in the retainer 400 according to the embodiment of the present invention having the above configuration will be described.

First, the grease flows through the through hole TH of the first retainer body 410 and the through hole TH of the second retainer body 420 . In addition, after the grease is introduced through the first central inlet hole 413 and the first side inlet hole 414 of the first retainer body 410 , the first central communication hole 413 - 1 communicates with the first side inlet hole 413 - 1 A portion of the grease flows into the first lower seating groove 412 through the ball 414 - 1 through the flow path FL, and the rest of the grease flows into the second central storage groove 425 - of the second retainer body 220 . 1) and the second side storage groove 426-1, and then flows into the second lower seating groove 422 through the flow path FL.

That is, when the pressure of the grease is temporarily increased due to an external impact, etc., and it is difficult to flow the grease only through the through hole TH, the grease is transferred to the first central inlet hole 413 of the first retainer body 410 and the first Grease is primarily introduced through the side inlet hole 414 . A portion of the introduced grease is introduced into the first lower seating groove 412 through the flow path FL, and is directed to an absorption part to be described later. The remainder of the introduced grease flows into the second central storage groove 425 - 1 and the second side storage groove 426 - 1 of the second retainer body 220 . The grease introduced into the second central storage groove 425-1 and the second side storage groove 426-1 flows into the second lower seating groove 422 through the flow path FL and flows into an absorption unit to be described later. do. That is, the grease, which is primarily introduced into the absorption part and secondarily flows into the second central storage groove 425-1 and the second side storage groove 426-1, is secondarily stored in the increased pressure. . Accordingly, even if the pressure of the grease temporarily rises, it can be absorbed.

Meanwhile, in the second retainer body 420 , similarly, after the grease is introduced through the second central inlet hole 423 and the second side inlet hole 424 of the second retainer body 420 , the second central communication hole Part of the grease flows into the second upper seating groove 421 through the flow path FL through the 413-1 and the second side communication hole 414-1, and the rest of the grease flows into the first retainer body 210. It flows into the first central storage groove 415-1 and the first side storage groove 416-1 of the first upper seating groove 411 through the flow path FL.

At this time, the grease may be introduced through the third inlet hole 425 of the second retainer body 420 , and the grease introduced through the third inlet hole 425 may pass through the third communication hole 427 . Part of the grease flows into the second upper seating groove 421 and the second lower seating groove 422 through the flow path FL and flows into the absorption part, and the rest of the grease flows into the third storage groove of the first retainer body 410 . After being introduced into the 417 , the first upper seating groove 411 and the first lower seating groove 312 are introduced through the flow path FL and are introduced into the absorption unit.

Hereinafter, the buffer unit 500 provided between the first retainer body 410 and the second retainer body 420 will be described with reference to FIGS. 14 to 19 .

The buffer unit 500 includes a first upper seating groove 411 and a first lower seating groove 412 of the first retainer body 410 and a second upper seating groove 421 of the second retainer body 420 . and the second lower seating groove 422 , respectively.

The buffer unit 500 includes an elastic storage unit 510 that expands and contracts when grease is introduced, a support ring 520 in which the elastic storage unit 510 is accommodated, and is provided in the support ring 520 . It includes a folding elastic part 530 that provides an elastic force to the elastic storage part 510 . That is, the elastic storage part 510 is respectively disposed in the four seating grooves 411 , 412 , 421 , 422 , and the support ring 520 and the folding elastic part 530 are disposed outside the elastic storage part 510 .

The elastic storage unit 510 includes a hollow elastic storage unit body 510 made of an elastic material, and an inlet/outhole 520 formed on one side of the elastic storage unit body 510 through which grease enters and exits. That is, the grease with an increased temporary pressure flows into the elastic storage unit body 510 using rubber or the like through the entry/exit hole 520 . When the pressure returns to the normal state, the grease stored in the elastic storage body 510 flows out to properly maintain the grease pressure inside the cross roller bearing of the present invention.

On the other hand, the elastic storage unit 510 is disposed inside the support ring 520, the support ring 520 has a ring shape, and the first support ring 521 and the second support ring 522 are spaced apart by a predetermined interval. includes A bar-shaped connection frame 523 is provided between the first support ring 521 and the second support ring 522 . The connection frame 523 is formed to be spaced apart from each other by a predetermined distance in the circumferential direction of the first support ring 521 or the second support ring 522 .

The foldable elastic parts 530 are disposed in the circumferential direction of the support ring 520 , are formed in a wavy shape, and are respectively disposed in spaces between the connection frames 523 . That is, as shown, the foldable elastic part 530 has a ∧ shape and is disposed in the circumferential direction. The folding elastic part 530 is disposed in the space of the connection frame 523 . In this case, the distance between the connecting frames 523 is longer than the horizontal distance in the ∧ shape of one unit among the folding elastic parts 530 . Due to this configuration, the foldable elastic part 530 may be expanded in the horizontal direction to respond to an increase in distance.

In addition, a portion of the foldable elastic part 530 in the circumferential direction is opened. This is so that when the elastic storage unit 510 expands, the foldable elastic part 530 comes in contact with the foldable elastic part 530 and unfolds, so that it can respond to a case where the distance increases accordingly. After the elastic storage part 510 is expanded, when the foldable elastic part 530 returns by the elastic force, the foldable elastic part 530 presses the elastic storage part 510 to release the expanded elastic storage part 510 . will bring it back

Meanwhile, a connection part 540 is provided between the elastic storage parts 510 . That is, even when the elastic storage part 510 is changed or the elastic storage part 510 on one side is rotated, it is absorbed to stably maintain the elastic storage part 510 .

The connection part 540 for this purpose includes a ring-shaped elastic part 541 and a cover 542 provided on both sides of the elastic part 541 and fixed to the elastic storage part 510 , respectively. In this case, the elastic part 541 includes an elastic arc part 5411 having an arc-shaped cross section having a specific circumferential length, and extension parts 5412 extending in the horizontal direction from both sides of the elastic arc part 5411. include The elastic arc portion 5411 may have an Ω shape as shown. The extension portion 5412 extends in the horizontal direction from both sides of the elastic arc portion 5411 .

The cover 542 is disposed inside the extension 5412 . The cover 542 includes a first cover 542A provided on one side of the elastic part 541 and a second cover 542A provided on the other side of the elastic part 542 and having a symmetrical shape of the first cover 542A. and a cover 542B. That is, the cover 542 is disposed on both sides of the elastic part 541, respectively, as shown in FIGS. 19 and 20 . The cover 542 has a symmetrical shape in the left-right direction, and the side surfaces of the cover 542 in the direction of the elastic part 541 are opened, respectively. That is, the cover 542 has a hollow shape and includes a cover body 5421 in which the direction of the elastic part 541 is opened. At this time, the interlocking protrusion 5422 protrudes on the cover body 5421 .

A first open portion 5413 formed in a circumferential direction is formed in the extension portion 5412 disposed on one side of the elastic portion 541 , the interlocking protrusion 5422 is inserted, and the other portion of the elastic portion 541 is inserted. A second opening portion 5414 formed in the direction of the elastic storage portion 510 is formed in the extension portion 5412 disposed on the side, and the interlocking protrusion 5422 is inserted thereinto.

That is, the first opening 5413 is formed in the circumferential direction, and the interlocking protrusion 5422 is inserted into the first opening 5413 . Accordingly, when the elastic storage part linked to the left cover 542A in the drawing rotates for some reason among the cover 542 , the left cover 542A in the drawing rotates, and at this time, the interlocking protrusion 5422 also rotates. However, since the interlocking protrusion 5422 rotates inside the first opening 5413, rotational displacement is limited. When the interlocking protrusion 5422 wants to rotate beyond the rotational displacement limited by the first opening 5413, the interlocking protrusion 5422 is caught on the inner surface of the first opening 5413 and the extension 5412. is linked and rotates. The extended part 5412 is integrally formed with the elastic arc part 5411 so that the elastic arc part 5411 also rotates, but the rotation range thereof is significantly reduced. Accordingly, even if the rotation of the elastic storage unit is within a certain range, the rotation is allowed, and if the rotation is over a certain range, the rotational displacement is elastically limited to achieve structural stability.

If the elastic storage part fluctuates, for example, when the elastic storage part increases, the interlocking protrusion 5422 is caught in the first opening 5413 , and the interlocking protrusion 5422 is also caught in the second opening 5412 . ) is caught, so when the space between the elastic storage parts increases, the elastic arc part 5411 becomes elastically wide and can respond to this. Conversely, when the gap between the elastic storage units is reduced, the elastic arc portion 5411 may be elastically flared to respond thereto.

As shown in FIG. 8 , when the pressure of the grease filled on one side of the retainer 400 temporarily increases, the grease flows through the through hole TH of the retainer 400 to lower the pressure at the portion where the temporary pressure rises. If the pressure is further increased, the grease is first introduced, for example, through the first central inlet hole 413 and the first side inlet hole 414 of the first retainer body 410 . A portion of the introduced grease is introduced into the first lower seating groove 412 through the flow path FL and is directed toward the absorption unit 500 . The remainder of the introduced grease flows into the second central storage groove 425 - 1 and the second side storage groove 426 - 1 of the second retainer body 220 .

The grease introduced into the second central storage groove 425-1 and the second side storage groove 426-1 flows into the second lower seating groove 422 through the flow path FL, and the absorption part 500 is introduced into That is, the grease is primarily introduced into the absorbing part 500 and secondarily introduced into the second central storage groove 425-1 and the second side storage groove 426-1, and the pressure is secondarily increased. temporarily save According to the present invention, even if the pressure of the grease temporarily rises, it can be absorbed.

The grease introduced into each of the seating grooves flows toward the absorption part 500 provided in each of the seating grooves. The grease is directed toward the elastic storage unit 510 through an open portion (part O in FIG. 15 ) of the foldable elastic portion 530 of the absorbent portion 500 . The grease directed toward the elastic storage unit 510 is introduced into the elastic storage unit 510 through the entry/exit hole 512 of the elastic storage unit 510 . The elastic storage unit 510 is expanded by the introduced grease. As shown in FIG. 17 , the expandable elastic storage part 510 presses the folding elastic part 530 so that the folding elastic part 530 is unfolded.

If the temporary pressure increases and the pressure of the grease decreases, the expanded elastic storage unit 530 compresses the expanded elastic storage unit 510 while returning by the elastic force, thereby filling the inside of the elastic storage unit 510 . The used grease is discharged through the inlet hole 512 . The discharged grease is discharged to the outside of the retainer 400 through the reverse process described above.

10: raw material supply unit 20: pyrolysis reactor
30: washing tower 40: condenser
61, 62 separator 70 purification tower
80: recycled oil recovery tank 90: sludge discharge part

Claims (7)

a raw material supply unit 10 for supplying a raw material mixture obtained by mixing the crushed waste synthetic resin particles and a pore filler filled in the voids between the waste synthetic resin particles to the pyrolysis reactor 20;
a pyrolysis reactor 30 for generating organic gas by thermally decomposing the raw material mixture supplied from the raw material supply unit 10;
a cleaning tower 30 for cleaning the organic gas generated in the pyrolysis reactor 20 to generate cleaned organic gas and deposits;
a condenser 40 for condensing the organic gas washed in the washing tower 30 to generate a condensate;
a first separator (61) for separating oil from the deposits generated in the washing tower (30);
a second separator 62 for separating oil from the condensate generated in the condenser 40; and
and a purification tower (70) for introducing the oil separated in the first separator (61) and the second separator (62) and performing fractional distillation to produce regenerated oil.
According to claim 1,
The raw material supply unit 10,
a crusher 13 for crushing the waste synthetic resin;
a mixer 14 for mixing the crushed waste synthetic resin particles with a pore filler; and
and a void filler supply line (L10) for supplying void filler to the mixer 14,
The purification tower 70,
a fractionation column 72 for fractionally distilling the oil introduced from the first separator 61 and the second separator 62 to separate the regenerated oil by grade; and
and a regenerated oil recovery line (L70) for recovering the regenerated oil separated in the fractionation column 72 by grade,
Among the regenerated oil separated in the fractionation column 72, the regenerated oil containing a C1 to C10 hydrocarbon-based compound can be used as a pore filler, and the regenerated oil recovery line L70 is a pore filler supply line L10 and An emulsifying device for waste synthetic resin, characterized in that it is connected.
According to claim 1,
The emulsifying device of the waste synthetic resin,
a first flow line (L11) connecting the pyrolysis reactor 20 and the cleaning tower 30 to supply the organic gas generated in the pyrolysis reactor 20 to the cleaning tower 30;
a second flow line (L12) connecting the cleaning tower (30) and the condenser (40) to supply the organic gas cleaned in the cleaning tower (30) to the condenser (40); and
It is connected to the side of the condenser 40, further comprising a third flow line (L13) for discharging the non-condensed organic gas that is not condensed in the condenser 40,
A heater 25 is installed in the first flow line L11 to maintain the organic gas supplied to the cleaning tower 30 at 200° C. to 250° C.,
The emulsification apparatus for waste synthetic resin, characterized in that the temperature of the organic gas flowing into the condenser 40 is maintained at 150° C. or higher, and the pressure in the condenser 40 is maintained at 10 kg/cm 2 or higher.
A mixing process of obtaining a raw material mixture by mixing the crushed waste synthetic resin particles and a pore filler filled in the voids between the waste synthetic resin particles;
a pyrolysis process of thermally decomposing the raw material mixture to generate an organic gas;
a cleaning process of cleaning the organic gas generated in the pyrolysis process to generate cleaned organic gas and deposits;
a condensation process of condensing the organic gas cleaned in the cleaning process to generate a condensate;
a first separation process of separating oil from deposits generated in the washing process;
a second separation process of separating oil from the condensate generated in the condensation process; and
and a purification process of fractionally distilling the oil separated in the first separation process and the second separation process to produce regenerated oil,
The pore filler is an emulsification method of a waste synthetic resin, characterized in that it comprises a C1-C10 hydrocarbon-based compound.
5. The method of claim 4,
The pore filler is an emulsification method of waste synthetic resin, characterized in that the regenerated oil produced in the refining process.
5. The method of claim 4,
The cleaning process is performed by introducing the organic gas generated in the thermal decomposition process to maintain it at 200°C to 250°C,
In the condensing process, the organic gas cleaned in the washing process is introduced into the condenser 40 , and then the condensed condensate is separated to the lower end of the condenser 40 , and the non-condensed organic gas is not condensed to the side of the condenser 40 . An emulsification method of waste synthetic resin, characterized in that it is separated into
7. The method of claim 6,
The condensation process is performed by maintaining the organic gas cleaned in the washing process at a temperature of 150° C. or higher, introducing it into the condenser 40, and maintaining the pressure of the condenser 40 at 10 kg/cm 2 or higher. emulsification method.

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