Catalytic cracking apparatus of refining system of pyrolysis oil

Abstract

The present invention relates to a catalytic cracking device for a high-quality light oil refining system for pyrolysis oil. It can be configured to be smart and compact so as to be easily applied to small-scale pyrolysis systems. Through a precise refining process, the pyrolysis oil (recycled oil) produced in the pyrolysis system can be reused as a general-purpose fuel, and economic efficiency can be secured by achieving high quality. Furthermore, using a new method, low-quality, high-viscosity mixed heavy oil can be continuously refined into high-quality light oil, and high-quality light oil can be obtained under relatively low temperature conditions. High-quality light oil can be manufactured in an economical and environmentally friendly manner. Finally, unstable elements, unsaturated hydrocarbons, sulfur compounds, chlorine compounds, etc., are removed using silica gel, etc., thereby producing high-quality light oil with a color of approximately ASTM No. 0.5 to 1.

Description

Technology Field

[0001] The present invention relates to a high-quality light oil refining system for pyrolysis oil, which refines pyrolysis oil (recycled oil) produced in a pyrolysis process of various hydrocarbon-based organic wastes such as waste lubricating oil, waste synthetic resin, and waste tires into high-quality light oil. More specifically, the invention relates to a catalyst cracking device for a high-quality light oil refining system for pyrolysis oil that can be configured to be smart and compact so as to be easily applied to small-scale pyrolysis systems, and can secure economic efficiency by producing high-quality and general-purpose light oil through a precise refining process by refining the pyrolysis oil produced in existing pyrolysis systems. Background Technology

[0002] Generally, plastic refers to a material that can be molded by heating, pressurizing, or both, or a synthetic resin made using such a material. Although the final product contains a large amount of molecular weight and chemical substances in a solid state, it is easy to mold as it has fluidity during molding, allowing for the production of various types of articles. Furthermore, as it is manufactured in a polymer form by polymerizing various materials using petroleum as the main raw material, it is possible to produce polymer compounds with various functions and characteristics by polymerizing materials that may have the characteristics desired by the user, and thus its applications and usage are rapidly increasing.

[0003] Furthermore, plastic is a type of petroleum compound that uses petroleum as its primary raw material. Because it is manufactured in a polymer form, it is difficult to decompose, resulting in excellent corrosion resistance that allows for long-term use. Additionally, it is easy to mold, enabling the production of various shapes, and due to its lightweight nature, its usage is rapidly increasing as it is applied in a wide range of products, from household goods to various industrial items.

[0004] However, plastics that are discarded after a single use are difficult to dispose of in landfills due to their non-biodegradability, and incineration releases various harmful gases that pollute the atmosphere, making it difficult to dispose of waste plastics.

[0005] Furthermore, as reserves of oil, including petroleum used as fuel for plastic production, shrink, oil prices are rising, and due to resource depletion, the need to reuse the oil contained within waste plastics is increasing.

[0006] Accordingly, methods for converting waste plastic into oil through pyrolysis are being developed to increase resource recycling rates by reducing and recovering the oil contained within the waste plastic.

[0007] In the method of pyrolysis oiling of waste plastics, when waste plastics are heated to about 400–500°C in an air-blocked state, the carbon bonds of the polymer are broken, producing pyrolysis gas and pyrolysis oil (recycled oil).

[0008] However, pyrolysis oil (recycled oil) produced from polyolefin waste plastics such as polyethylene (PE) and polypropylene (PP) contains large amounts of tar components, large amounts of wax components, and organic hazardous compounds, most notably high concentrations of chlorine components. Furthermore, contaminants and foreign substances other than waste plastics are fed directly into the pyrolysis reactor without undergoing a pretreatment process and undergo pyrolysis. As a result, it is a very low-grade oil that cannot serve as a general-purpose fuel, so it is necessary to improve the quality and economic viability of recycled oil through a precise refining process.

[0009] The most critical factor preventing the pyrolysis process technology for waste plastics from establishing itself as an economically viable industry from the early 1970s to the present is that the produced recycled oil lacks versatility as fuel oil. Improving the quality of recycled oil is a very urgent task, but there is a limitation in that large-scale facility investment, like that of general petrochemical companies, is impossible due to the characteristics of the recycled oil refining process.

[0010] Refining technology for recycled oil must be on par with major-level technology, but there is an urgent need to smarten and compact the refining technology so that it can be applied to small-scale pyrolysis plants.

[0011] Conventional refining technology for recycled oil is mainly limited to decolorization and the removal of impurities through distillation, and high-quality refined oil cannot be obtained through a simple distillation process alone. It can be said that there is no special effect from such distillation other than the removal of residual carbon tar and decolorization. Since this simple distillation lacks a hydrocarbon cracking process, wax components remain in the recycled oil, and the pour point of the recycled oil is considerably high. Consequently, the recycled oil solidifies even in slight cold during the spring, autumn, and winter seasons, which is a drawback that makes the recycled oil unsuitable for general use.

[0012] Furthermore, while the removal of chlorine and sulfur components among residual organic hazardous compounds is a fundamental requirement of recycled oil refining technology, conventional refining techniques lack processes for removing or neutralizing these components. Consequently, chlorine remains in the recycled oil, leading to a significant decline in the quality of the produced refined oil. This results in serious technical limitations, such as the phenomenon where using such degraded refined oil in industrial burners causes the burner nozzle to melt within a short period of time. Prior art literature

[0013] Korean Published Patent No. 10-2011-0088058 (August 3, 2011) Korean Published Patent No. 10-2012-0019346 (March 6, 2012) The problem to be solved

[0014] The present invention was developed to improve upon the aforementioned problems. The first objective of the present invention is to provide a catalytic cracking device for a high-quality light oil purification system of pyrolysis oil that can be reused as a general-purpose fuel, which can be configured to be smart and compact enough to be applied to small-scale pyrolysis systems. This is achieved by first pre-treating impurities from pyrolysis oil (recycled oil) through a pre-treatment process, then heating and distilling (vaporizing) the pyrolysis oil pre-treated through a light oil stripping process, followed by carrying out a catalytic cracking process (catalytic cracking decomposition reaction) and a fractional distillation process in stages to break the bonds of high-molecular-weight hydrocarbons and finally purify high-quality light oil of low-molecular-weight hydrocarbons (C5~C11).

[0016] The second problem that the present invention aims to solve is to provide a catalyst cracking device for a high-quality light oil refining system for pyrolysis oil, which can extend the lifespan of the reactor by effectively preventing coking inside the reactor in advance, by introducing separated heavy oil into the reactor and continuously supplying it in a circulating manner while heating the heavy oil introduced into the reactor by a reactor piping heater installed outside the reactor.

[0018] The third problem that the present invention aims to solve is to provide a catalytic cracking device for a high-quality light oil refining system for pyrolysis oil, in which a two-stage tray is installed inside a catalytic cracking column, a specific catalyst is placed in a certain amount on the tray, and dechlorination can be performed using a catalyst that has the function of neutralizing dechlorination, and the surface of the tray is formed in a corrugated shape to expand the contact area between gas and oil and further enhance the catalytic tracking reaction.

[0020] The technical problems of the present invention are not limited to those mentioned above, and other unmentioned technical problems will be clearly understood by those skilled in the art from the description below. means of solving the problem

[0021] To achieve the above objective, the method for refining high-quality light oil from pyrolysis oil according to the present invention comprises: a pretreatment step of transferring pyrolysis oil (recycled oil) into a pretreatment tank, adding a coagulant into the pretreatment tank, and maintaining it at a constant temperature to separate and remove impurities (e.g., sludge, moisture, pyrolysis gas, etc.) contained in the pyrolysis oil; an oil-water separation step of separating and removing moisture contained in the pyrolysis oil that has undergone the pretreatment step; a light oil stripping step of storing the pyrolysis oil in a distillation column (distillation tower), heating and distilling it to separate heavy oil from light oil (LGO), and storing it in a heavy oil storage tank; and a catalytic cracking step of supplying the heavy oil in the heavy oil storage tank into a reactor and heating and distilling it at 350~400℃, while separating high molecular weight hydrocarbons into low molecular weight hydrocarbons by a catalyst while passing it through a catalytic cracking column (catalytic cracking tower) installed at the top of the reactor. The technical features include: a fractional distillation step in which low molecular weight hydrocarbons generated during the catalyst cracking step are heated and distilled to fractionally distill light gas oil (LGO) and light diesel oil (LDO), and the light gas oil and light diesel oil are stored in a light gas oil tank and a light diesel oil tank, respectively; and a final purification step in which the light gas oil in the light gas oil tank and the light diesel oil in the light diesel oil tank are passed through a filter filled with solid silica gel (or silica gel / activated carbon) to finally purify the impurities contained in the light gas oil and light diesel oil.

[0023] Furthermore, the high-quality light oil refining method for pyrolysis oil according to the present invention has a technical feature comprising an exhaust gas purification step in which the refined light gas oil and light diesel oil are stored in a light gas oil storage tank and a light diesel oil storage tank, respectively, and the non-condensing gas generated in the light gas oil storage tank and the light diesel oil storage tank is purified by passing through a gas buffer tank and a gas purification tank, then passes through an adsorption tower to undergo UV (ultraviolet) photodecomposition to remove odors, and then discharged into the atmosphere.

[0025] In addition, in the light oil stripping step, a packing bed is installed in multiple stages inside the distillation column, and the heavy oil and light oil are separated by heating and distilling at 160 to 180°C.

[0027] In addition, during the catalyst cracking step, a reactor heating condenser is connected and installed on the outside of the reactor, and the heavy oil introduced into the reactor is heated by the reactor heating condenser and continuously supplied in a circulating manner, thereby preventing coating phenomena inside the reactor in advance and extending the lifespan of the reactor.

[0028] In the above catalyst cracking step, the heavy oil can be heated and distilled at 350 to 400°C in the kettle of the reactor.

[0030] Furthermore, in the above pretreatment step, sodium hydroxide (NaOH) can be added as a coagulant to the pretreatment tank and heated to 90 to 100°C to separate and remove impurities contained in the pyrolysis oil.

[0031] In the above pretreatment step, a flexible treatment process is enabled by providing a pretreatment tank, taking into account flow rate fluctuations due to discontinuous supply and demand of recycled oil and the stability of downstream facilities.

[0032] After the coagulant is introduced into the pretreatment tank, it can be heated to 90~100℃ using a heating boiler to remove moisture and volatile impurities, and the viscosity of the high-viscosity recycled oil can be lowered to increase the efficiency of membrane purification.

[0034] Furthermore, in the fractional distillation step, the vapor generated at the upper side of the fractional distillation column is liquefied by passing through a light gas oil reflux condenser and stored in a light gas oil tank, and some of the light gas oil in the light gas oil tank can be reintroduced into the fractional distillation column by a reflux pump.

[0035] The vapor generated at the lower side of the fractional distillation column is liquefied by passing through a light diesel oil reflux condenser and stored in a light diesel oil tank, and some of the light diesel oil in the light diesel oil tank can be reintroduced into the fractional distillation column by a reflux pump.

[0037] Meanwhile, the high-quality light oil refining system for pyrolysis oil according to the present invention comprises: a pretreatment tank linked to a pyrolysis process for storing pyrolysis oil (recycled oil) generated through the pyrolysis process and for separating and removing impurities contained in the pyrolysis oil by adding a coagulant and heating for a pretreatment process; an oil-water separator for separating and removing moisture contained in the pyrolysis oil; a light oil stripper for stripping heavy oil and light oil from the pyrolysis oil by heating and distilling the pyrolysis oil; a heavy oil storage tank for storing the heavy oil generated during the light oil stripping process; a reactor for heating and distilling the heavy oil supplied from the heavy oil storage tank; a reactor piping heater connected to the outside of the reactor and circulating the heavy oil introduced into the reactor while heating it; and a catalytic cracking device (unit) installed on the upper side of the reactor and performing catalytic cracking to separate high molecular weight hydrocarbons of the heavy oil into low molecular weight hydrocarbons. The technical features include: a fractional distillation unit that heat-distills low molecular weight hydrocarbons generated during the above-mentioned catalytic cracking process to fractionally distill them into light gas oil (LGO) and light diesel oil (LDO); a light gas oil tank that stores the light gas oil generated at the upper side of the fractional distillation column, separated by the fractional distillation column; a light diesel oil tank that stores the light diesel oil generated at the lower side of the fractional distillation column, separated by the fractional distillation column; and a final purification unit that finally removes impurities contained in the light gas oil and light diesel oil by allowing the light gas oil in the light gas oil tank and the light diesel oil in the light diesel oil tank to pass through a filter filled with solid silica gel (or silica gel / activated carbon).

[0039] Furthermore, the high-quality light oil refining system for pyrolysis oil according to the present invention has a technical feature comprising: an exhaust gas purification unit in which non-condensing gas evaporating from a light gas oil storage tank for storing refined light gas oil and a light diesel oil storage tank for storing refined light diesel oil is purified by passing through a gas buffer tank and a gas purification tank, then passes through an adsorption tower to undergo UV (ultraviolet) photodecomposition to remove odors, and then discharged into the atmosphere.

[0041] In addition, a plurality of trays are arranged sequentially at regular intervals vertically in an alternating manner within the fractional distillation column of the fractional distillation unit, and the surface of the trays may be formed in a corrugated shape. Effects of the invention

[0042] As explained above, the present invention has the following effects.

[0043] First, it can be configured to be smart and compact so as to be easily applied to small-scale pyrolysis systems, and by refining the pyrolysis oil (recycled oil) produced from the pyrolysis system through a precise refining process, it can be reused as a general-purpose fuel and achieve high quality, thereby ensuring economic viability.

[0044] Second, using a new process, low-quality, high-viscosity mixed heavy oil is continuously refined into high-quality light oil, and high-quality light oil can be obtained under relatively low temperature conditions, enabling the production of high-quality light oil in an economical and environmentally friendly manner.

[0045] Third, the pyrolysis oil (recycled oil) produced in the pyrolysis system is first subjected to a pretreatment process to separate and remove impurities contained in the pyrolysis oil, and then the pyrolysis oil is heated and distilled (vaporized) through a light oil stripping process to separate the light oil and heavy oil. After separating the heavy oil, the separated heavy oil is fed into the reactor, and the heavy oil introduced into the reactor is heated by a reactor piping heater installed outside the reactor while being continuously supplied in a circulating manner, thereby effectively preventing coking inside the reactor in advance and extending the lifespan of the reactor.

[0046] Fourth, a two-stage tray is installed inside the catalytic cracking column, and a specific catalyst is placed in the tray in a certain amount. Dechlorination can be performed using a catalyst that has the function of neutralizing dechlorination, and the surface of the tray is formed in a corrugated shape to increase the contact area between gas and oil, thereby further enhancing the catalytic tracking reaction.

[0047] Fifth, by using silica gel or the like to finally remove unstable elements, unsaturated hydrocarbons, sulfur compounds, chlorine compounds, etc., it is possible to produce high-quality light oil with a color of approximately ASTM No. 0.5 to 1.

[0048] Sixth, after liquefying the oil vapor generated in the fractional distillation process through a reflux condenser, a portion of the light gas oil is returned to the fractional distillation column by a reflux pump, while the remaining light gas oil is sent to a light gas oil tank for storage, and a portion of the light diesel oil is returned to the fractional distillation column, while the remaining light diesel oil is sent to a light diesel oil tank for storage; thereby, the fractional distillation effect can be further enhanced, and high-quality light oil can be produced.

[0050] The effects of the present invention are not limited to those mentioned above, and other unmentioned effects will be clearly understood by those skilled in the art from the description in the claims. Brief explanation of the drawing

[0051] FIG. 1 is a flowchart illustrating the entire method for refining high-quality light oil from pyrolysis oil according to an embodiment of the present invention. FIGS. 2A and 2B are drawings illustrating the entire high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 3 is a conceptual diagram illustrating the entire method for refining high-quality light oil from pyrolysis oil according to an embodiment of the present invention. FIG. 4 is a schematic diagram illustrating a pretreatment tank in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 5 is a schematic diagram illustrating an oil-water separator in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 6 is a schematic diagram illustrating a light oil stripper in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 7 is a schematic diagram illustrating a heavy oil storage tank in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 8 is a schematic diagram illustrating a reactor and a catalytic cracking device in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 9 is a schematic diagram illustrating a fractional distillation unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 10 is a schematic diagram illustrating a final refining unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 11 is a schematic diagram illustrating an exhaust gas purification unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 12 is a perspective view showing a packing bed in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention. FIG. 13 is a perspective view illustrating an Opirus corrugate-shaped filler in the catalytic cracking device of the present invention. Specific details for implementing the invention

[0052] Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the attached drawings so that a person skilled in the art to which the present invention pertains can easily practice the present invention.

[0053] In describing the embodiments thereof, technical details that are well known in the art to which the present invention pertains and are not directly related to the present invention are omitted. This is intended to convey the essence of the present invention more clearly without obscuring it by omitting unnecessary explanations. For the same reason, some components in the accompanying drawings are exaggerated, omitted, or schematically depicted.

[0054] In addition, the size of each component does not entirely reflect its actual size. Identical or corresponding components in each drawing have been assigned the same reference number.

[0056] A method for refining high-quality light oil from pyrolysis oil according to a preferred embodiment of the present invention involves first separating and removing impurities contained in the pyrolysis oil (recycled oil) produced in a pyrolysis system through a pretreatment process, and then separating the light oil and heavy oil by heating and distilling (vaporizing) the pyrolysis oil through a light oil stripping process, and then introducing the separated heavy oil into a reactor. In this method, the heavy oil introduced into the reactor is heated by a reactor heating condenser installed outside the reactor and continuously supplied in a circulating manner, thereby effectively preventing coking inside the reactor in advance.

[0057] Next, by carrying out the catalytic cracking process (catalytic cracking decomposition reaction) and the fractional distillation process in stages, the bonds of high-molecular-weight hydrocarbons are broken, thereby enabling the refining of high-quality light oil containing low-molecular-weight hydrocarbons (C5–C11). During the catalytic cracking and fractional distillation processes, the high-molecular-weight hydrocarbon chains of the oil vapor (C20–C25) are cracked and converted into oil vapor particles of light oil containing low-molecular-weight hydrocarbons.

[0059] Furthermore, during the final refining process, the light gas oil in the light gas oil tank and the light diesel oil in the light diesel oil tank are passed through a filter filled with solid silica gel to remove impurities contained in the light gas oil and light diesel oil, thereby allowing them to be refined into high-purity light oil.

[0060] The high-purity light oil of the present invention has passed all 20 test items of the operating oil (lubricant) standard of the Korea Petroleum Management Agency and received a passing grade, and the silica gel filter, which is a filler used to purify the residue contained in the light oil, can be used semi-permanently through a drying process after washing with a non-flammable organic solvent.

[0062] Hereinafter, with reference to the attached drawings, a method and system for refining high-quality light oil from pyrolysis oil according to an embodiment of the present invention will be described.

[0063] FIG. 1 is a flowchart illustrating the entire high-quality light oil refining method of pyrolysis oil according to an embodiment of the present invention, FIG. 2a and FIG. 2b are drawings illustrating the entire high-quality light oil refining system of pyrolysis oil according to an embodiment of the present invention, and FIG. 3 is a conceptual diagram illustrating the entire high-quality light oil refining method of pyrolysis oil according to an embodiment of the present invention.

[0064] FIG. 4 is a schematic diagram illustrating a pretreatment tank in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, FIG. 5 is a schematic diagram illustrating an oil-water separator in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, and FIG. 6 is a schematic diagram illustrating a light oil stripper in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention.

[0065] FIG. 7 is a schematic diagram illustrating a heavy oil storage tank in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, FIG. 8 is a schematic diagram illustrating a reactor and a catalyst cracking unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, FIG. 9 is a schematic diagram illustrating a fractional distillation unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, FIG. 10 is a schematic diagram illustrating a final refining unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, and FIG. 11 is a schematic diagram illustrating an exhaust gas purification unit in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention.

[0066] And FIG. 12 is a perspective view illustrating a packing bed in a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention, and

[0067] FIG. 13 is a perspective view illustrating an opirus corrugate-shaped filler in the catalytic cracking device of the present invention.

[0068] First, as illustrated in FIGS. 1 to 3, the high-quality light oil refining method of pyrolysis oil according to an embodiment of the present invention has technical features comprising: a pretreatment step (S110) for receiving and pretreating pyrolysis oil (recycled oil) produced in a pyrolysis system (1); an oil-water separation step (S120) for separating pyrolysis oil and water (water); a light oil stripping step (S130) for separating heavy oil and light oil from pyrolysis oil; a catalytic cracking step (S140) for separating high molecular weight hydrocarbons into low molecular weight hydrocarbons by a catalyst; a fractional distillation step (S150) for separating light gas oil and light diesel oil from light oil; a final refining step (S160) for finally refining impurities contained in light gas oil and light diesel oil; and an exhaust gas purification step (S170) for removing harmful substances generated during the refining process and then discharging exhaust gas.

[0070] Hereinafter, a method for refining high-quality light oil from pyrolysis oil according to an embodiment of the present invention will be described in detail step by step with reference to FIGS. 1 to 3.

[0071] First, in the above pretreatment step (S110), the pyrolysis oil (recycled oil) containing sludge, moisture, foreign substances, pyrolysis gas, etc. generated in the pyrolysis system (1) can be bypassed as is and pumped by the pump (P3) to be transferred into the pretreatment tank (110) for storage. After adding a coagulant (or adsorbent) into the pretreatment tank (110), the temperature is maintained at a constant level to separate and remove impurities (e.g., sludge, moisture, gas, etc.) contained in the pyrolysis oil. The coagulant is stored in the coagulant tank (111) and is introduced into the pretreatment tank (110) by pumping with the pump (P4).

[0072] In the above pretreatment step (S110), sodium hydroxide (NaOH) is added as an example of a coagulant into the pretreatment tank (110), and then the temperature is maintained at 90 to 100°C to separate and remove impurities contained in the pyrolysis oil.

[0073] By using a coagulant, sulfur oxides can be effectively removed from oil fractions containing sulfur oxides, thereby increasing the breakthrough adsorption amount or breakthrough drainage of sulfur oxides.

[0074] When using coagulants, not only can sulfur oxide concentrations be maintained at levels low enough to satisfy environmental regulations, but operating costs can also be reduced, thereby increasing the economic efficiency of the entire purification process.

[0076] Next, in the oil-water separation step (S120), the moisture contained in the pyrolysis oil that has undergone the pretreatment step (S110) is separated and removed. The pyrolysis oil from which moisture has been removed is transferred back into the distillation column (131). The removed moisture (including some oil) is discharged to the outside by pumping of the pump (P5) along the discharge line (L1).

[0078] Next, in the light oil stripping step (S130), the pyrolysis oil is transferred and stored in a distillation column (131), and then heated and distilled by a heater (135) to separate the heavy oil and light oil, after which the heavy oil is transferred and stored in a heavy oil storage tank (140).

[0079] The heavy oil is stored in a heavy oil storage tank (140) to be transferred to the next stage (S140), and the separated light oil is separated by a light oil condenser (137) along a separate transfer line (L2), then stored in a light oil storage tank (138), and then transferred to the fractional distillation process described later (indicated as ① in FIG. 2a and 2b) by pumping of a pump (P6).

[0080] In the above light oil stripping step (S130), a packing bed (10) (see FIG. 12) is installed in multiple stages (e.g., 6 stages) inside a distillation column (131), and heavy oil and light oil are separated by heating and distilling at 160 to 180°C.

[0082] Next, in the catalyst cracking step (S140), the heavy oil in the heavy oil storage tank (140) is supplied into the reactor (150) and heated and distilled at 350 to 400°C, while passing through the catalyst cracking column (161) installed at the top of the reactor (150) to separate the high molecular weight hydrocarbons into low molecular weight hydrocarbons through the cracking reaction of the catalyst (163).

[0083] The vaporized oil vapor, heated in the reactor (150), contains other heavy oils such as light oil components and wax components, and a low-molecular-weight hydrocarbon cracking reaction process is carried out in the catalytic cracking column (or catalytic cracking tower) (161) through the function of the catalyst (163).

[0084] The light oil produced through the cracking reaction is transferred to the next process, the fractional distillation process (indicated as ① in FIG. 2a and FIG. 2b).

[0085] In the catalyst cracking column (161), a multi-stage tray (162), for example, two stages, may be installed. The tray (162) may be installed, for example, in the middle layer and the bottom layer, and a specific catalyst (163) may be placed in the tray (162) in a certain amount. In the top layer of the catalyst cracking column (catalyst cracking tower) (161), a packing material (165) in the shape of an opirus corrugator may be placed to ensure maximum contact with oil vapor. At this time, a catalyst having a neutralizing function for dechlorination may be used to perform dechlorination. The temperature at this time may be controlled, for example, at 180 to 230°C, and may separate gasoline, kerosene, diesel fuel, etc., and secondarily, some water mixed with oil. The surface of the tray (162) may be formed in a corrugated shape to expand the contact area between gas and oil, thereby further enhancing the catalyst tracking reaction.

[0086] In the above catalyst cracking step (S140), a reactor piping heater (155) is installed outside the reactor (150), and the heavy oil introduced into the reactor (150) is heated by the reactor piping heater (155) and continuously supplied in a circulating manner, thereby effectively preventing coking inside the reactor (150) in advance and extending the lifespan of the reactor (150).

[0087] The heating method by the above reactor piping heater (155) can be selected from a first method of heating to 240°C or lower and a second method of raising the temperature to 240°C to 430°C.

[0088] First, the above first method forcibly circulates the heavy oil introduced into the reactor (150) through the reactor piping heater (155) using a circulation pump (P1), and uses the pressure difference generated by the forced circulation to prevent coking inside (inner wall) of the catalyst cracking column (catalyst tower) (161).

[0089] And the second method above raises the temperature using a ceramic heater (161a) wrapped around the outer circumference of the reactor (150) to vaporize the heavy oil components, thereby causing cracking to occur in the catalytic process.

[0091] Next, in the fractional distillation step (S150), the low molecular weight hydrocarbon generated during the catalyst cracking step (S140) is heated and distilled to fractionally distill light gas oil (LGO) and light diesel oil (LDO), and then the light gas oil and light diesel oil are temporarily stored in the light gas oil tank (T1) and the light diesel oil tank (T2), respectively.

[0092] In the fractional distillation step (S150) above, the vapor generated at the upper side of the fractional distillation column (171) is liquefied by passing through the light gas oil reflux condenser (C1) and then stored in the light gas oil tank (T1), and some of the light gas oil in the light gas oil tank (T1) is reintroduced into the fractional distillation column (171) by the reflux pump (P2).

[0093] The oil vapor generated at the lower side of the fractional distillation column (171) passes through a light diesel oil reflux condenser (C2) to be liquefied and then stored in a light diesel oil storage tank (T2). Although not shown in the drawing, some of the light diesel oil in the light gas oil tank (T2) can be reintroduced into the fractional distillation column (171) by a reflux pump (P2).

[0094] In other words, at the top of the fractional distillation column (171), the generated vapor is liquefied through a reflux condenser (C1), and then a portion of the light gas oil is returned to the fractional distillation column (171) by a reflux pump (P2), while the remaining light gas oil is sent to a light gas oil tank (T1) for storage.

[0095] By installing a packing bed (10) (see FIG. 12) in multiple stages inside the fractional distillation column (171), the fractional distillation effect can be further enhanced.

[0096] At the bottom of the fractional distillation column (171), the generated oil vapor is liquefied through a reflux condenser (C2) and stored in a light diesel tank (T2). In the reheating boiler (183), a portion of the light diesel is reheated and converted into oil vapor, which is then sent back to the fractional distillation column (171) for fractional distillation, and the remaining light diesel is sent from the reheating boiler (183) to the light diesel tank (T2) for storage.

[0098] Next, in the final purification step (S160), the light gas oil in the light gas oil tank (T1) and the light diesel oil in the light diesel oil tank (T2) are passed through a filter (192) filled with solid silica gel (or silica gel / activated carbon) to finally remove impurities (e.g., sulfur oxides, chlorine compounds, and unsaturated hydrocarbons) contained in the light gas oil and light diesel oil.

[0099] The light gas oil and light diesel oil are configured to pass through the filter (192) by pumping of the pump (P7).

[0101] Finally, in the exhaust gas purification step (S170), the purified light gas oil and light diesel oil are stored in the light gas oil storage tank (181) and the light diesel oil storage tank (182), respectively. The non-condensing gas generated in the light gas oil storage tank (181) and the light diesel oil storage tank (182) is purified by passing through the gas buffer tank (196) and the gas purification tank (197), then passes through the adsorption tower (198) to undergo UV (ultraviolet) photodecomposition to remove odors, and is then discharged into the atmosphere through the blower fan (199).

[0103] Hereinafter, with reference to FIGS. 2a, 2b, and 3, a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention will be described. In the drawings, the unexplained reference numeral P refers to a conventional pump that pumps a fluid (e.g., pyrolysis oil or light oil, etc.).

[0104] As illustrated in FIGS. 2a, 2b, and 3, a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention comprises: a pretreatment tank (110) for receiving and pretreating pyrolysis oil (recycled oil) produced in a pyrolysis system (1); an oil-water separator (120) for separating pyrolysis oil and water (water); a light oil stripper (130) for separating heavy oil and light oil; a heavy oil storage tank (140) for storing the separated heavy oil; a reactor (150) for heating and distilling the heavy oil supplied from the heavy oil storage tank (140); a reactor piping heater (155) connected to the outside of the reactor (150) and circulating the heavy oil introduced into the reactor while heating it; and a catalyst cracking device (160) installed on the upper side of the reactor (150) and performing catalyst cracking to separate high molecular weight hydrocarbons into low molecular weight hydrocarbons. The technical features include: a fractional distillation unit (170) that heat-distills the light oil of low molecular weight hydrocarbons generated through the above-mentioned catalytic cracking process to separate it into light gas oil (LGO) and light diesel oil (LDO); a light gas oil tank (T1) for temporarily storing the light gas oil; a light diesel oil tank (T2) for temporarily storing the light diesel oil; a final refining unit (190) for producing high-quality light oil; and an exhaust gas purification unit (195) for preventing the emission of pollutants into the atmosphere.

[0106] Hereinafter, the components of a high-quality light oil refining system for pyrolysis oil according to an embodiment of the present invention will be described in detail.

[0107] First, as shown in FIGS. 2a, 3, and 4, the pretreatment tank (110) is linked to the pyrolysis process to bypass and store the pyrolysis oil produced through the pyrolysis process, and after adding a coagulant for the pretreatment process, maintains it at a constant temperature to primarily separate and remove impurities contained in the pyrolysis oil.

[0108] Here, the pyrolysis oil (recycled oil) containing sludge, moisture, foreign substances, pyrolysis gas, etc. generated in the pyrolysis system (1) is bypassed as is and pumped by the pump (P3) to be transferred into the pretreatment tank (110) for storage.

[0109] Sodium hydroxide (NaOH) is added as a coagulant or adsorbent into the pretreatment tank (110) and maintained at 90 to 100°C to effectively separate and remove impurities (sludge, moisture, gas, etc.) contained in the pyrolysis oil. The coagulant is stored in the coagulant tank (111) and is introduced into the pretreatment tank (110) by pumping with the pump (P4).

[0111] Additionally, as illustrated in FIGS. 2a, 3, and 5, the oil-water separator (120) separates and removes moisture contained in the pyrolysis oil. The separated pyrolysis oil is transferred to a light oil stripper (130), and the removed moisture (including some oil) is collected in a storage tank (122) and then discharged to the outside by pumping of a pump (P5) along a separate discharge line (L1).

[0113] Additionally, as illustrated in FIGS. 2a, 3, and 6, the light oil stripper (130) strips the heavy oil and light oil by heating and distilling the pyrolysis oil. The pyrolysis oil is transferred and stored in a distillation column (131), and after separating the heavy oil and light oil by heating and distilling with a heater (135), the heavy oil is stored in a heavy oil storage tank (140). A packing bed (10) (see FIG. 12) is installed in multiple stages (e.g., 6 stages) inside the distillation column (131), and the light oil is separated by using a weak vacuum pump (about 0.1 MPa) (not shown), by heating and distilling at 160 to 180°C to separate the heavy oil and light oil.

[0114] The separated heavy oil is stored in a heavy oil storage tank (140) to be transferred to the next process (catalytic cracking reaction process), and the separated light oil is separated by a light oil condenser (137) along a separate transfer line (L2) and then stored in a light oil storage tank (138), after which it can be transferred to the fractional distillation process (indicated as ① in FIG. 2a and FIG. 2b) described later by pumping of a pump (P6).

[0116] Additionally, as shown in FIGS. 2a, 3, and 8, the reactor (150) heats and distills the heavy oil supplied from the heavy oil storage tank (140).

[0117] The catalytic cracking unit (160) of the present invention is installed above the reactor (150) and performs a catalytic cracking reaction to separate high molecular weight hydrocarbons into low molecular weight hydrocarbons. The light oil produced through the cracking reaction is transferred to the next process, the fractional distillation process (indicated by ① in FIG. 2a and FIG. 2b).

[0118] The catalytic cracking process plays a critical role in refining facilities. To separate high-molecular-weight hydrocarbons into low-molecular-weight hydrocarbons, the selection of the catalyst and the associated temperature range and pressure settings are critical. To convert heavy oil components into light oil by selecting an appropriate catalyst and establishing corresponding conditions, a systematic structure that considers catalyst function and production yield must be synergized to maximize performance.

[0119] To this end, two trays (162) may be installed in an alternating manner within the catalyst cracking column (161). The two trays (162) may be installed in the middle and bottom layers of the catalyst cracking column (161), and a certain amount of a specific catalyst (163) is placed in the trays (162).

[0120] In the uppermost layer of the catalyst cracking column (catalytic cracking tower) (161), an opirus corrugated packing material (165) (see FIG. 2a and FIG. 13) may be placed so that oil vapor comes into maximum contact.

[0121] At this time, dechlorination can be performed using a catalyst that has the function of neutralizing dechlorination. The surface of the tray (162) is formed in a corrugated shape to increase the contact area between the gas and oil, thereby further enhancing the catalytic tracking reaction.

[0122] The heating method by the above-mentioned reactor piping heater (155) can be selected from a first method of heating to about 180°C to 240°C or lower and a second method of raising the temperature to about 240°C to 430°C.

[0123] First, the above first method forcibly circulates the heavy oil introduced into the reactor (150) through the reactor piping heater (155) using a circulation pump (P1), and prevents coking inside the catalyst cracking column (catalyst tower) (161) by utilizing the pressure difference generated by the forced circulation. At this time, the catalyst cracking temperature can be controlled at 180℃ to 240℃, and separates gasoline, kerosene, diesel oil, some water mixed with secondary oil, etc.

[0124] The gas, which is heated and converted into oil vapor, passes through a catalytic cracking column (catalytic cracking tower) (161) installed at the top of the reactor (150), and through the role of a catalyst, the heavy oil component having a chain-like structure of high-molecular-weight hydrocarbons is separated into a light oil component having low-molecular-weight hydrocarbons.

[0125] And the second method above raises the temperature using a ceramic heater (161a) wrapped around the outer circumference of the reactor (150) to vaporize the heavy oil components, thereby causing cracking to occur in the catalytic process. In this way, the high-temperature heating method required for vaporizing the heavy oil components is heated to about 240°C to 430°C by a ceramic heater (161a) wrapped around the outer circumference of the reactor (150) so that the heavy oil components are uniformly vaporized, and the vapor passes through the catalytic cracking column (or catalytic cracking tower) and, through the role of a catalyst, separates the heavy oil components having high molecular weight hydrocarbons with a chain structure into light oil components having low molecular weight hydrocarbons.

[0126] In the above catalyst cracking process, a reactor piping heater (155) is installed outside the reactor (150), and the heavy oil introduced into the reactor (150) is heated by the reactor piping heater (155) and continuously supplied in a circulating manner, thereby effectively preventing coking inside the reactor (150) in advance and extending the lifespan of the reactor (150).

[0127] The light oil produced after the cracking reaction following the separation of low molecular weight hydrocarbons in the catalyst cracking unit (160) is transferred to the fractional distillation unit (170), and the residual sludge is automatically transferred to the sludge storage tank (168) through the vacuum pump (167).

[0129] Additionally, as illustrated in FIGS. 2b, 3, and 9, the fractional distillation unit (170) heat-distills low molecular weight hydrocarbons produced through a catalytic cracking process to fractionally distill light gas oil (LGO) and light diesel oil (LDO). The light gas oil (LGO) and light diesel oil (LDO) produced through the fractional distillation process are transferred into the light gas oil tank (T1) and the light diesel oil tank (T2), respectively, and stored.

[0130] The light gas oil tank (T1) stores the light gas oil generated at the upper side of the fractional distillation column (171) by being separated by the fractional distillation unit (170).

[0131] The light diesel oil tank (T2) stores light diesel oil generated at the lower side of the fractional distillation column (171) that is separated by the fractional distillation unit (170).

[0132] In the above fractional distillation process, the vapor generated at the upper side of the fractional distillation column (171) is liquefied by passing through a light gas oil reflux condenser (C1) and then stored in a light gas oil tank (T1), and some of the light gas oil inside the light gas oil tank (T1) is reintroduced into the fractional distillation column (171) by a reflux pump (P2).

[0133] The oil vapor generated at the lower side of the fractional distillation column (171) passes through a light diesel oil reflux condenser (C2) to be liquefied and then stored in a light diesel oil storage tank (T2). Although not shown in the drawing, some of the light diesel oil in the light gas oil tank (T2) can be reintroduced into the fractional distillation column (171) by a reflux pump (P2).

[0134] In other words, at the top of the fractional distillation column (171), the generated vapor is liquefied through a reflux condenser (C1), and then a portion of the light gas oil is returned to the fractional distillation column (171) by a reflux pump (P2), while the remaining light gas oil is sent to a light gas oil tank (T1) for storage.

[0135] By installing a packing bed (10) (see FIG. 12) in multiple stages inside the fractional distillation column (171), the fractional distillation effect can be further enhanced.

[0136] At the bottom of the fractional distillation column (171), the generated vapor is liquefied through a reflux condenser (C2) and stored in a light diesel tank (T2). In the reheating boiler (183), a portion of the light diesel is reheated and converted into vapor, which is then sent back to the fractional distillation column (171) for fractional distillation, and the remaining light diesel is sent from the reheating boiler (183) to the light diesel tank (T2) for storage.

[0138] As illustrated in FIG. 2b, FIG. 3 and FIG. 9, the tray-type fractional distillation unit (170) of the present invention may be composed of a fractional distillation column (171), a plurality of trays (172) installed inside the fractional distillation column (171), and reflux condensers (C1)(C2) installed in a reflux line (L1).

[0139] Inside the fractional distillation column (171), hot oil vapor flows from the bottom to the top and liquid light oil flows from the top to the bottom, and through thousands of distillation reaction contacts between gas and oil during the fractional distillation process, the substances are converted into light gas oil (LGO) and light diesel oil (LDO).

[0140] In the fractional distillation process, the upper part can be divided into a recitifying section and a stripping section, centered on the input section inside the fractional distillation column (171).

[0141] At the bottom of the fractional distillation column (171), the generated oil vapor is liquefied through a reflux condenser (C2) and stored in a light diesel tank (T2). In the reheating boiler (183), a portion of the light diesel oil is reheated and converted into oil vapor, which is then sent back to the fractional distillation column (171) for fractional distillation, and the remaining light diesel oil is sent from the reheating boiler (183) to the light diesel tank (T2) for storage.

[0142] At the top of the fractional distillation column (171), the generated vapor is liquefied through a reflux condenser (C1), and then a portion of the light gas oil is returned to the fractional distillation column (171) by a reflux pump (P2), while the remaining light gas oil is sent to a light gas oil tank (T1) for storage.

[0143] Inside the fractional distillation column (171), a plurality of trays (172) (shown in FIG. 9) are arranged sequentially at a constant vertical interval, and the surface of the trays (172) is formed in a corrugated shape, thereby allowing for the repeated optimal exchange of gas and oil, and cracking and separating light oils of different properties through the upper line, side line, and lower line. With this structure, it is possible to produce high-quality light oil with low viscosity and a low pour point.

[0145] Additionally, as illustrated in FIGS. 2b, 3, and 10, the final purification unit (190) allows the light gas oil from the light gas oil tank (T1) and the light diesel oil from the light diesel oil tank (T2) to pass through a filter (192) filled with solid silica gel (or silica gel / activated carbon) to finally purify impurities contained in the light gas oil and light diesel oil, such as sulfur oxides, chlorine compounds, and unsaturated hydrocarbons. A method is used in which the light gas oil and light diesel oil pass into a silica gel tank (191) that stores a plurality of filters (192) filled with solid silica gel (or silica gel / activated carbon).

[0147] Finally, as illustrated in FIGS. 2b, FIGS. 3, and FIGS. 11, the exhaust gas purification unit (195) purifies non-condensing gas (approximately 2%) generated in a light gas oil storage tank (181) that stores refined light gas oil and a light diesel oil storage tank (182) that stores refined light diesel oil, by passing through a gas buffer tank (196) and a gas purification tank (197), then passes through an adsorption tower (198) to undergo UV (ultraviolet) photodecomposition to remove odors, and then discharges it into the atmosphere through a blower fan (199). With this configuration, clean gas is stably discharged into the atmosphere.

[0149] As explained above, the present invention has the following effects.

[0150] First, it can be configured to be smart and compact so as to be easily applied to small-scale pyrolysis systems, and by refining the pyrolysis oil (recycled oil) produced from the pyrolysis system through a precise refining process, it can be reused as a general-purpose fuel and achieve high quality, thereby ensuring economic viability.

[0151] Second, using a new process, low-quality, high-viscosity mixed heavy oil is continuously refined into high-quality light oil, and high-quality light oil can be obtained under relatively low temperature conditions, enabling the production of high-quality light oil in an economical and environmentally friendly manner.

[0152] Third, the pyrolysis oil (recycled oil) produced in the pyrolysis system is first subjected to a pretreatment process to separate and remove impurities contained in the pyrolysis oil, and then the pyrolysis oil is heated and distilled (vaporized) through a light oil stripping process to separate the light oil and heavy oil. After separating the heavy oil, the separated heavy oil is fed into the reactor, and the heavy oil introduced into the reactor is heated by a reactor heating condenser installed outside the reactor while being continuously supplied in a circulating manner, thereby effectively preventing coking inside the reactor in advance and extending the lifespan of the reactor.

[0153] Fourth, a two-stage tray is installed inside the catalytic cracking column, and a specific catalyst is placed in the tray in a certain amount. Dechlorination can be performed using a catalyst that has the function of neutralizing dechlorination, and the surface of the tray is formed in a corrugated shape to increase the contact area between gas and oil, thereby further enhancing the catalytic tracking reaction.

[0154] Fifth, by using silica gel or the like to finally remove unstable elements, unsaturated hydrocarbons, sulfur compounds, chlorine compounds, etc., it is possible to produce high-quality light oil with a color of approximately ASTM No. 0.5 to 1.

[0155] Sixth, after liquefying the oil vapor generated in the fractional distillation process through a reflux condenser, a portion of the light gas oil is returned to the fractional distillation column by a reflux pump, while the remaining light gas oil is sent to a light gas oil tank for storage, and a portion of the light diesel oil is returned to the fractional distillation column, while the remaining light diesel oil is sent to a light diesel oil tank for storage, thereby further enhancing the fractional distillation effect and enabling the production of high-quality light oil.

[0157] Meanwhile, the present specification and drawings disclose preferred embodiments of the present invention. Although specific terms have been used, they are used merely in a general sense to facilitate the explanation of the technical content of the present invention and to aid in understanding the invention, and are not intended to limit the scope of the present invention. It is obvious to those skilled in the art that, in addition to the embodiments disclosed herein, other variations based on the technical concept of the present invention are possible. Explanation of the symbols

[0158] 1: Pyrolysis system (device) 10: Packing bed 110: Pretreatment tank 120: Oil-water separator 130: Light oil stripper 131: Distillation Column 135: Heater 140: Heavy oil storage tank 150: Reactor 155: Reactor Piping Heater 160: Catalytic cracking device (unit) 161: Catalytic cracking column (or catalytic cracking tower) 162: Tray 163: Catalyst 165: Opirus corrugated-shaped filler 167: Vacuum pump 168: Sludge storage tank 170: Fractional distillation unit 171: Fractional distillation column 181: Light gas oil storage tank 182; Light diesel storage tank 190: Final Refining Unit 191: Silica gel tank 192: Filter 195: Exhaust gas purification unit 196: Gas buffer tank 197: Gas purification tank 198: Adsorption tower C1: Light gas oil reflux condenser C2: Light diesel fuel recirculation condenser T1: Light gas oil tank T2: Light diesel fuel tank

Claims

Claim 1 A pretreatment tank (110) for storing pyrolysis oil (recycled oil) generated through the pyrolysis process in conjunction with the pyrolysis process, and for separating and removing impurities contained in the pyrolysis oil by adding a coagulant and heating for a pretreatment process; an oil-water separator (120) for separating and removing water contained in the pyrolysis oil that has undergone the pretreatment process; a light oil stripper (130) for stripping heavy oil and light oil from the pyrolysis oil by heating and distilling the pyrolysis oil that has undergone the oil-water separation process; a heavy oil storage tank (140) for storing heavy oil generated during the light oil stripping process; and a reactor (150) for heating and distilling the heavy oil supplied from the heavy oil storage tank (140). A reactor piping heater (155) connected to the outside of the reactor (150) and circulating the heavy oil flowing into the reactor (150) while heating it, or a ceramic heater (161a) wrapped around the outer circumference of the reactor (150) to raise the temperature and vaporize the heavy oil components to cause cracking; a fractional distillation unit (170) that heats and distills the light oil of low molecular weight hydrocarbons generated during the catalytic cracking process to fractionally distill it into light gas oil (LGO) and light diesel oil (LDO); a light gas oil tank (T1) that stores the light gas oil generated at the upper side of the fractional distillation column (171) separated by the fractional distillation unit (170); and a light diesel oil tank (T2) that stores the light diesel oil generated at the lower side of the fractional distillation column (171) separated by the fractional distillation unit (170). and a final purification unit (190) that allows the light gas oil of the light gas oil tank (T1) and the light diesel oil of the light diesel oil tank (T2) to pass through a filter (192) filled with solid silica gel to finally purify the impurities contained in the light gas oil and light diesel oil;A catalytic cracking device of a high-quality light oil refining system for pyrolysis oil, comprising: a reactor (150) installed on the upper side thereof, and performing catalytic cracking to separate high molecular weight hydrocarbons into low molecular weight hydrocarbons; wherein a two-stage tray (162) is installed in the middle and bottom layers of the catalytic cracking column (161) such that the surface is formed in a corrugated shape to expand the contact area between gas and oil and improve the catalytic cracking reaction; wherein an opirus corrugated packing material (165) is arranged in the uppermost layer of the catalytic cracking column (161) to maximize contact with oil vapor; and wherein the reactor piping heater (155) is installed outside the reactor (150) and continuously supplies the heavy oil flowing into the reactor (150) in a forced circulation manner using a circulation pump (P1) while heating the heavy oil introduced into the reactor (150), thereby preventing coking of the inner wall of the catalytic cracking column (161) by utilizing the pressure difference generated by the forced circulation. Claim 2 delete Claim 3 delete Claim 4 delete Claim 5 A catalytic cracking device of a high-quality light oil refining system for pyrolysis oil, characterized in that, in claim 1, the light oil produced by undergoing a cracking reaction after separation of low molecular weight hydrocarbons in the catalytic cracking unit (160) is transferred to the fractional distillation unit (170), and the residual sludge is automatically transferred to a sludge storage tank (168) through a vacuum pump (167). Claim 6 delete

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