Method for manufacturing petroleum product

Abstract

To provide: a method for manufacturing a petroleum product obtained by processing raw oil in a petroleum refining facility, by which it is possible to reduce consumption of fossil fuel compared to a conventional manufacturing method; and a manufacturing system for a petroleum product.SOLUTION: A method for manufacturing a petroleum product is intended to manufacture the petroleum product by processing raw oil in a petroleum refining facility. Energy obtained by burning either one or both of a combustible material including waste and methane obtained from waste is used as energy necessary for the processing.SELECTED DRAWING: None

Description

[Technical field]

[0001] The present invention relates to a process for producing a petroleum product. [Background technology]

[0002] From the perspective of creating a recycling-oriented society, it is necessary to effectively use recyclable resources while reducing the consumption of limited natural resources. To reduce the consumption of natural resources, there is a demand to reduce the consumption of non-renewable natural resources and to reuse and recycle used natural resources.

[0003] From this perspective, the development of waste recycling technology is one of the important issues in terms of the increase in waste in recent years and the need to curb the consumption of natural resources. Among waste recycling technologies, there is a high demand for recycling technology for waste plastics, which are produced from fossil fuels, which are natural resources.

[0004] There are three main methods for recycling waste plastic: material recycling, in which waste plastic is reused as is; chemical recycling, in which waste plastic is chemically broken down to recover basic chemical raw materials such as monomers; and thermal recycling, in which thermal energy is recovered from waste plastic.

[0005] In chemical recycling, waste plastics are converted into other chemical substances and reused, for example by pyrolyzing them at high temperatures to produce chemical raw materials such as synthetic gas or decomposed oil, or by chemically decomposing them to produce monomers. Compared to material recycling, this has the advantage that it is often possible to recycle plastics even if they contain a mixture of different types of plastics or contain foreign matter or dirt.

[0006] As a chemical recycling method, Patent Document 1 discloses a method for cracking a hydrocarbon polymer (resin) in a fluid catalytic cracking unit. Specifically, the method discloses a method for cracking a hydrocarbon polymer, characterized in that a mixture of a hydrocarbon polymer and a hydrocarbon oil selected from fluid catalytic cracking gasoline, light cracked gas oil, heavy cracked gas oil, and cracked residual oil is mixed with a fluid catalytic cracking feedstock oil and supplied to a fluid catalytic cracking unit. [Prior art documents] [Patent documents]

[0007] [Patent Document 1] JP 2002-294251 A Summary of the Invention [Problem to be solved by the invention]

[0008] Energy such as electricity and steam required for the decomposition treatment described in Patent Document 1 is still produced from fossil fuels, which are natural resources. Therefore, the method described in Patent Document 1 is also insufficient from the viewpoint of reducing consumption of natural resources.

[0009] The present invention has been made in consideration of the above-mentioned circumstances, and has an objective of providing a method for producing petroleum products by processing raw oil in an oil refining facility, and a system for producing petroleum products, which can reduce consumption of fossil fuels compared to conventional production methods. [Means for solving the problem]

[0010] In order to solve the above problems, the present invention has the following aspects. [1] A method for producing petroleum products by processing feedstock oil in an oil refining facility, in which the energy required for the processing is obtained by burning either or both of combustible materials, including waste, and methane obtained from the waste. [2] The method for producing a petroleum product described in [1], wherein the raw material oil contains a resin derived from waste plastic. [3] A method for producing a petroleum product described in [1] or [2], in which combustion of either or both of the combustible materials including the waste and the methane obtained from the waste is carried out outside the refinery facility. [4] The method for producing a petroleum product according to any one of [1] to [3], wherein the waste is general waste. [5] A petroleum product production system comprising: an oil refining facility; a combustion facility that combusts either or both of combustible materials including waste and methane obtained from the waste; and a means for transmitting energy obtained by the combustion facility between the combustion facility and the oil refining facility. Effect of the Invention

[0011] According to the present invention, it is possible to provide a method for producing petroleum products by processing feed oil in an oil refining facility, and a system for producing petroleum products, which can reduce consumption of fossil fuels compared to conventional production methods. [Brief description of the drawings]

[0012] [Figure 1] 1 is a configuration diagram showing the configuration of a petroleum product production system according to one embodiment of the present invention. [Diagram 2] 1 is a configuration diagram showing a configuration of an oil refining facility according to an embodiment of the present invention. [Diagram 3] FIG. 1 is a configuration diagram showing the configuration of a refining facility for refining cracked oil according to one embodiment of the present invention. [Figure 4] FIG. 1 is a schematic diagram showing how to determine the Hansen solubility parameter value and the interaction radius. [Diagram 5] 1 is a schematic diagram showing the distance between the solubility parameter values ​​of two substances, substance 1 and substance 2. [Figure 6] FIG. 2 is a schematic diagram showing a case where the relative energy difference between substance 1 and substance 2 based on the Hansen solubility parameters is within 1. [Figure 7]FIG. 2 is a schematic diagram showing a case where the relative energy difference between substance 1 and substance 2 based on the Hansen solubility parameters is greater than 1. [Figure 8] 1 is a schematic diagram showing the relationship between the Hansen solubility parameter of a solvent L, the Hansen spheres S(PA1) and S(PA2) of resins PA1 and PA2, and the Hansen spheres S(PB1) and S(PB2) of resins PB1 and PB2. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0013] The following describes in detail the embodiments of the present invention. However, the following description is an example of an embodiment of the present invention, and the present invention is not limited to these contents and can be modified and implemented within the scope of its gist.

[0014] As used herein, "feedstock" refers to crude oil-derived fractions, waste-derived resins, and mixtures thereof that are typically processed in various petroleum refineries. As used herein, "petroleum products" refers to petrochemical products such as liquefied petroleum gas, gasoline, naphtha, kerosene, jet fuel, diesel, lubricating base oil, heavy oil, asphalt, and aromatic compounds and olefins, which are produced in various oil refining facilities. In this specification, "waste" includes both general waste and industrial waste. Industrial waste is classified into 20 types as specified by law (Waste Disposal and Public Cleansing Act), and general waste refers to waste other than industrial waste. However, "waste" in this specification does not include waste such as waste liquid generated in the oil refining process of refinery facilities. In other words, "waste" in this specification means industrial waste excluding general waste and waste generated in the oil refining process of refinery facilities.

[0015] In the petroleum product production method of this embodiment, petroleum products are produced by processing feedstock oil in an oil refining facility. The petroleum product production method of this embodiment uses energy obtained by burning either or both of combustible materials including waste and methane obtained from the waste as the energy required for the processing. First, the petroleum product production system used in the petroleum product production method of this embodiment will be described.

[0016] <Petroleum product manufacturing system> The oil product production system of this embodiment comprises an oil refining equipment, a combustion equipment that combusts either or both of combustible materials including waste and methane obtained from the waste, and a means for transmitting energy obtained by the combustion equipment between the combustion equipment and the oil refining equipment. The means for transmitting energy refers to the form of energy (steam, electricity) for transmitting the energy obtained by the combustion equipment, as well as piping between the combustion equipment and the oil refining equipment, etc. for transmitting the energy obtained by the combustion equipment.

[0017] 1 is a configuration diagram showing the configuration of a petroleum product production system according to one embodiment of the present invention. The petroleum product production system 100 of this embodiment includes an oil refining facility 101 and a combustion facility 102. The petroleum product production system 100 of this embodiment may further include a microbial treatment facility 103 and a power generation facility 104.

[0018] <Combustion equipment> The combustion equipment 102 is an equipment that burns either or both of combustible materials including waste and methane obtained from the waste, and produces steam by utilizing the heat obtained. The combustion equipment 102 is connected to the oil refinery equipment 101 via a steam supply line L201. The combustion equipment 102 is connected to the power generation equipment 104 via a steam supply line L204. The combustion equipment 102 is connected to the microbial treatment equipment 103 via a methane supply line L302. As the combustion equipment, a conventionally known combustion equipment can be used. An example of the combustion equipment is a combustion equipment equipped with a garbage pit, a crane, an incinerator, a waste heat boiler, an economizer, an ash pit, a dust collector, and a denitrification reaction tower. The functions of each of the above devices equipped in the combustion equipment will be described later.

[0019] <Power generation facilities> The power generation facility 104 is a facility that generates power by using the steam produced by the combustion facility 103. The power generation facility 104 is connected to the oil refinery facility 101 via a power supply line L401. As the power generating equipment, a conventionally known power generating equipment can be used. One example of the power generating equipment is a steam turbine type power generating equipment.

[0020] <Microbial treatment equipment> The microbial treatment facility 103 is a facility that produces methane by methane fermentation of food waste. The microbial treatment facility 103 is connected to the oil refinery facility 101 via a methane supply line L301. As the microbial treatment equipment, a conventionally known microbial treatment equipment can be used. An example of the microbial treatment equipment is a microbial treatment equipment equipped with a separator, a slurry tank, a methane fermentation tank, and a desulfurization tower. The functions of each of the above devices equipped in the microbial treatment equipment will be described later.

[0021] <Oil refining equipment> The oil refining facility 101 is a facility for producing oil products by processing raw oil. The oil refining facility 101 is not particularly limited, but may be an atmospheric distillation facility, a vacuum distillation facility, a fluid catalytic cracking facility, a heavy oil thermal cracking facility, a direct desulfurization facility, an indirect desulfurization facility, a kerosene desulfurization facility, a catalytic reforming facility, an isomerization facility, a hydrocracking facility, or the like. It is preferably a facility for cracking hydrocarbons, more preferably a fluid catalytic cracking facility, a heavy oil thermal cracking facility, or a hydrocracking facility, and most preferably a fluid catalytic cracking facility. A fluid catalytic cracking facility (hereinafter also referred to as "FCC facility") comprises a riser that produces cracked oil containing petroleum products by contacting the feedstock oil with a fluid catalytic cracking catalyst to crack the feedstock oil, a reaction tower that separates the cracked oil from the fluid catalytic cracking catalyst, a regeneration tower that regenerates the catalyst by burning the carbon (coke) that has accumulated on the separated fluid catalytic cracking catalyst, and a refining facility.

[0022] An example of an FCC facility will be described below with reference to Fig. 2. Fig. 2 is a configuration diagram showing an example of an FCC facility. The FCC facility 1 includes a riser 10, a reaction tower 20, a regeneration tower 30, and a purification facility 40.

[0023] (Riser) The riser 10 is an apparatus for producing a cracked oil containing petroleum products by contacting a feedstock with a fluid catalytic cracking catalyst and cracking the feedstock. The riser 10 is connected to, for example, a regenerated catalyst transfer line 34 for supplying a fluid catalytic cracking catalyst regenerated in the regenerator 30 and a fluid catalytic cracking feedstock supply line 11 for supplying a fluid catalytic cracking feedstock. When a feedstock containing a resin solution as described below is used as the feedstock, the riser 10 is preferably connected to a resin solution supply line 51 for supplying the resin solution. A preheater 12 and a preheater 52 are provided on the fluid catalytic cracking feedstock supply line and the resin solution supply line, respectively. Furthermore, the upper part of the riser 10 is connected to a reaction tower 20.

[0024] (Reaction tower) The reaction tower 20 is a device for separating the cracked oil from the fluid catalytic cracking catalyst. The reaction tower 20 includes, for example, a cyclone 21, a cracked oil discharge line 22, a stripper 23, and a post-reaction catalyst transfer line 24. The upper part of the cyclone 21 is connected to the cracked oil discharge line 22. Furthermore, the bottom of the stripper 23 and the lower part of the regeneration tower 30 are connected by the post-reaction catalyst transfer line 24.

[0025] (Regeneration Tower) The regenerator 30 is an apparatus for regenerating the catalyst by burning the coke on the fluid catalytic cracking catalyst separated in the reaction tower 20. The regenerator 30 includes, for example, an air blower 31, an air grid 32, a cyclone 33, a regenerated catalyst transfer line 34, and an exhaust gas line 35. The bottom of the regenerator and the air blower 31 are connected via the air grid 32. Furthermore, a cyclone 33 is installed at the top of the regenerator, and the upper part of the cyclone 33 is connected to the exhaust gas line 35.

[0026] (Refining equipment) The refining equipment 40 is an equipment for separating cracked oil containing petroleum products produced in the fluid catalytic cracking unit into individual products. As shown in FIG. 3, the refining equipment includes, for example, a distillation tower 41, a line 42, a distillation tower 43, a line 44, a distillation tower 45, a line 46, a distillation tower 47, a line 48, an aromatics extraction unit 60, a line 61, a line 62, a naphtha cracker 70, and a catalytic reforming unit 80. The distillation tower 41 is connected to the reaction tower 20 via a cracked oil discharge line 22 near the middle of the tower. The distillation tower 43 is connected to the top of the distillation tower 41 via a line 42 near the middle of the tower. The distillation tower 45 is connected to the bottom of the distillation tower 43 via a line 44 near the middle of the tower. The distillation tower 47 is connected to the top of the distillation tower 45 via a line 46 near the middle of the tower. The aromatics extraction unit 60 is connected to the bottom of the distillation tower 45 via a line 48. The naphtha cracker 70 is connected to the aromatics extraction unit 60 via a line 61. The catalytic reformer 80 is connected to the aromatics extraction unit 60 via line 62 .

[0027] The distillation towers 41, 43, 45, and 47 may be distillation towers known in the art depending on the objects to be separated, as described below. The aromatics extraction unit 60 may be aromatics extraction units known in the art depending on the objects to be separated, as described below. Similarly, the naphtha cracker 70 and the catalytic reformer 80 may be naphtha crackers and catalytic reformers known in the art. Although the detailed structures of the reflux line, preheater, bottoms withdrawal line, effluent withdrawal line, and the like of the distillation tower are not shown in Fig. 3, as described above, the distillation tower has a structure known in the art. The same is true for the aromatics extraction unit, naphtha cracker, and catalytic reformer.

[0028] (Resin melting tank) When using a feedstock oil containing a resin solution as described below as the feedstock oil, the method for producing a petroleum product of this embodiment preferably includes a resin solution production step in which a resin is dissolved in advance to obtain a resin solution. In the resin solution production step, a specific resin is not dissolved from a mixture containing multiple types of resins, and resins other than the specific resin are dissolved to produce a resin solution. The resin dissolution tank 50 is an apparatus for carrying out a resin solution production process in which a mixture containing multiple types of resins, which will be described later, is left without dissolving a specific resin, and resins other than the specific resin are dissolved to produce a resin solution. An oil storage tank can be used as the resin dissolving tank. The resin dissolving tank 50 is connected to the riser 10 through a resin dissolving liquid supply line 51. The resin dissolving tank 50 is preferably equipped with a stirrer, a dissolving tank heater, a solid matter separator, and the like.

[0029] <Fluid catalytic cracking catalyst> The FCC facility is equipped with a fluidized catalytic converter (hereinafter also referred to as "FCC catalyst"). The FCC catalyst of the present embodiment preferably contains a zeolite such as a zeolite having a sodalite cage structure, β zeolite, or ZSM-5 type zeolite, and more preferably contains a zeolite having a sodalite cage structure. The content of the zeolite relative to the total mass of the FCC catalyst is preferably from 25 to 45 mass%, more preferably from 28 to 42 mass%, and further preferably from 30 to 40 mass%.

[0030] In this specification, zeolite having a sodalite cage structure means a zeolite having a sodalite cage structure, i.e., an aluminum and silicon tetrahedron as a basic unit, with each vertex of a three-dimensional regular octahedral crystal structure formed by sharing oxygen at the vertices with aluminum or silicon, and having voids formed by a tetradecahedral crystal structure defined by four-membered rings, six-membered rings, etc., and having various pore structures, skeletal densities, and channel structures by changing the locations and methods at which these sodalite cages are bonded to each other.

[0031] The zeolite having the sodalite cage structure may be one or more selected from sodalite, A-type zeolite, EMT, X-type zeolite, Y-type zeolite, stabilized Y-type zeolite, etc., and is preferably stabilized Y-type zeolite.

[0032] Stabilized Y-type zeolite is synthesized using Y-type zeolite as a starting material, and is more resistant to deterioration of crystallinity than Y-type zeolite. It is generally produced by subjecting Y-type zeolite to steam treatment at high temperatures several times, and then, if necessary, treating it with a mineral acid such as hydrochloric acid, a base such as sodium hydroxide, a salt such as calcium fluoride, or a chelating agent such as ethylenediaminetetraacetic acid. The stabilized Y-type zeolite obtained by the above method can be used in a form that has been ion-exchanged with a cation selected from hydrogen, ammonium, or polyvalent metals. Also, as the stabilized Y-type zeolite, a heat shock crystalline aluminosilicate zeolite (see Japanese Patent No. 2544317), which has a higher stability, can be used.

[0033] The FCC catalyst of the present embodiment preferably further contains a binder, a clay mineral, and the like. An example of the binder is silica sol. By using silica sol, the moldability during granulation of the FCC catalyst is improved, and it is possible to easily form the catalyst into a spherical shape. In addition, the flowability and abrasion resistance of the granulated FCC catalyst can be easily improved. The content of the binder relative to the total mass of the FCC catalyst is preferably 15 to 35 mass%, more preferably 18 to 32 mass%, and even more preferably 20 to 30 mass%.

[0034] Examples of clay minerals include montmorillonite, kaolinite, halloysite, bentonite, attapulgite, bauxite, etc. In the FCC catalyst of this embodiment, known inorganic oxide fine particles used in normal FCC catalysts, such as silica, silica-alumina (excluding the above-mentioned zeolite), alumina, silica-magnesia, alumina-magnesia, phosphorus-alumina, silica-zirconia, and silica-magnesia-alumina, can be used in combination with the above clay minerals. The sum of the contents of the clay mineral and the inorganic oxide relative to the total mass of the FCC catalyst is preferably 35 to 55 mass%, more preferably 38 to 52 mass%, and further preferably 40 to 50 mass%. The content of the clay mineral relative to the total mass of the FCC catalyst is preferably 25 to 50 mass %, more preferably 30 to 45 mass %, and even more preferably 32 to 42 mass %.

[0035] The FCC catalyst of the present embodiment may also contain a zeolite stability improver. The zeolite stability improver has a function of suppressing the collapse of zeolite crystals. Examples of the zeolite stability improver include phosphorus-based zeolite stability improvers such as phosphoric acid, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, aluminum monophosphate, and other water-soluble phosphates, and rare earth metal-based zeolite stability improvers such as scandium, yttrium, lanthanum, cerium, praseodymium, neodymium, samarium, gadolinium, dysprosium, and holmium. When the FCC catalyst contains a zeolite stability improver, the content of the zeolite stability improver relative to the total mass of the FCC catalyst is preferably 0.1 to 5 mass%.

[0036] The FCC catalyst is granulated to a certain size and then used in the fluid catalytic cracking reaction. The particle size of the FCC catalyst is not particularly limited as long as it is a particle size that can be used in a normal fluid catalytic cracking reaction, but the particle size is preferably within the range of 20 to 150 μm. The particle size of the FCC catalyst can be measured, for example, by using a micro-type electromagnetic vibration sieve, Model M-2, manufactured by Tsutsui Rikagaku Kikai Co., Ltd.

[0037] <Method of manufacturing fluid catalytic cracking catalyst> The FCC catalyst of the present embodiment can be produced by a conventionally known method. When the FCC catalyst contains zeolite, a binder, a clay mineral, and a zeolite stability improver, it can be produced by drying a slurry containing a predetermined amount of each of the zeolite, the binder, the clay mineral, and the zeolite stability improver.

[0038] In this production method, first, an aqueous slurry containing zeolite, a binder, a clay mineral, and a zeolite stability improver is prepared. The solid content of the aqueous slurry is preferably 5 to 60% by mass, more preferably 10 to 50% by mass. When the solid content of the aqueous slurry is within the above range, the amount of water evaporated during drying of the aqueous slurry becomes appropriate, and drying can be easily performed. In addition, the slurry can be easily transported without increasing its viscosity.

[0039] The aqueous slurry is then dried to obtain the microspheres. The aqueous slurry is preferably dried using a spray dryer under conditions of a gas inlet temperature of 200 to 600°C and a gas outlet temperature of 100 to 300°C.

[0040] In the present production method, the microspheres obtained by the above-mentioned drying treatment may be further subjected to washing treatment and ion exchange treatment by known methods, if necessary, to remove excess alkali metals and soluble impurities, etc., carried over from the various raw materials.

[0041] Specifically, the washing treatment can be carried out with water or aqueous ammonia. By washing with water or aqueous ammonia, the content of soluble impurities can be reduced.

[0042] Specifically, the ion exchange treatment can be carried out using an aqueous solution of an ammonium salt such as ammonium sulfate or ammonium sulfite, and this ion exchange can reduce the amount of alkali metals such as sodium and potassium remaining in the microspheres.

[0043] The above-mentioned washing treatment is usually carried out prior to the ion exchange treatment, but the ion exchange treatment may be carried out first, so long as the washing treatment and the ion exchange treatment are carried out suitably.

[0044] The above-mentioned washing treatment and ion exchange treatment are preferably carried out until the content of alkali metals and the content of soluble impurities are reduced to the desired levels or less. By reducing the content of alkali metals and the content of soluble impurities to the desired levels or less, the catalytic activity can be improved.

[0045] The microspheres preferably have an alkali metal content of 1.0% by mass or less, more preferably 0.5% by mass or less, and a soluble impurity content of 2.0% by mass or less, more preferably 1.5% by mass or less, based on the dry catalyst.

[0046] The microspheres that have been subjected to the above-mentioned washing and ion exchange treatments are preferably dried again at a temperature of 100 to 500° C. until the moisture content of the microspheres reaches 1 to 25% by mass. In this manner, the FCC catalyst of this embodiment can be produced.

[0047] <Production methods of petroleum products> In the method for producing oil products according to the present embodiment, oil products are produced by processing feedstock oil in an oil refinery facility. The energy required for the processing is obtained by burning either or both of combustible materials including waste and methane obtained from the waste. Below, we will explain the process of processing raw oil in an oil refinery and the process of obtaining energy from waste.

[0048] <Processing of raw oil in oil refinery facilities> The process of processing the feedstock oil in the oil refinery will be described in detail below, taking the case where the oil refinery is an FCC facility as an example. The process of processing the feedstock oil in the FCC facility includes a fluid catalytic cracking reaction process in which the feedstock oil is processed in the FCC facility. The feedstock oil may be a feedstock oil to be subjected to a normal fluid catalytic cracking reaction (hereinafter also referred to as "fluid catalytic cracking feedstock oil"). A resin derived from waste material, or a mixture thereof, and preferably contains a resin derived from waste material. In addition, as a resin derived from waste material, a resin derived from waste plastic is preferable. When the feedstock oil contains a resin derived from waste plastic, it becomes possible to recycle the waste plastic into a petroleum product, and the consumption of fossil fuels can be further suppressed. The following description will be given on the assumption that the feedstock oil contains a resin derived from waste plastics, but the feedstock oil may be only a fluid catalytic cracking feedstock oil or only a resin derived from waste plastics.

[0049] In the process of treating the feedstock oil in the present embodiment with the FCC facility, it is preferable to have a resin solution production process, prior to the fluid catalytic cracking reaction process, in which a resin solution is obtained by dissolving resins other than the specific resin without dissolving a specific resin from a mixture containing multiple types of resins contained in the waste plastic.

[0050] (Resin solution manufacturing process) In the resin solution manufacturing process of the present embodiment, a resin solution is manufactured by dissolving a resin other than the specific resin without dissolving a specific resin from a mixture containing a plurality of types of resins. In the present embodiment, it is preferable to select a solvent having a relative energy difference based on the Hansen solubility parameter for the specific resin of more than 1 and a relative energy difference based on the Hansen solubility parameter for the resin other than the specific resin of 1 or less, and to manufacture a resin solution by contacting the mixture with the solvent to dissolve the resin other than the specific resin. Hereinafter, the method for determining the Hansen solubility parameter and the relative energy difference will be described.

[0051] Hansen solubility parameters The Hansen solubility parameter (hereinafter simply referred to as "HSP") is based on the idea that two substances with similar intermolecular interactions are likely to dissolve in each other. The HSP is composed of the energy derived from intermolecular dispersion forces (δd), the energy derived from intermolecular dipole interactions (δp), and the energy derived from intermolecular hydrogen bonds (δh). These three parameters can be considered as coordinates in a three-dimensional space (Hansen space).

[0052] The HSP value of an evaluation sample whose HSP value is unknown can be calculated by the following method. HSP value (δd m , δp m , δh m) in three-dimensional space, multiple pure substances (substances consisting of one type of compound) with known HPS values ​​are plotted in the Hansen Solubility Parameter space. The Hansen Sphere is then specified based on the solubility of the evaluation sample in the pure substances, and the central value of the Hansen Sphere is determined to calculate the HSP value of the evaluation sample (Hansen Sphere method). The HSP value of the evaluation sample can also be calculated from information on the average molecular structure using the atomic group contribution method. In both the Hansen sphere method and the group contribution method, the HSP value of the evaluation sample can be calculated using, for example, computer software Hansen Solubility Parameters in Practice (HSPiP). In the case of the Hansen ball method, the evaluation sample may be a pure substance or a mixture.

[0053] A method for determining the central values ​​of the Hansen sphere, that is, the HSP values ​​(δdm, δpm, δhm), will be described with reference to FIG. First, the HSP values ​​of about 15 to 30 pure substances having known HSP values ​​are plotted in the three-dimensional space (coordinate axes are the dispersion force term δd, the dipole-dipole force term δp, and the hydrogen bond force term δh) illustrated in FIG. At this time, for example, pure substances that show solubility in the evaluation sample are indicated by a circle, and pure substances that do not show solubility in the evaluation sample are indicated by an X, as shown in Figure 4. Next, based on the plotted solubilities of the evaluation samples, the Hansen sphere S (shown as a sphere in Figure 4) is determined to be the one with the smallest radius among the imaginary spheres that include the pure substances that show solubility (shown by a circle in Figure 4) and do not include the pure substances that do not show solubility (shown by an X in Figure 4). The radius of the Hansen sphere S (the minimum radius) is the interaction radius R that dissolves the pure substance shown by the circle in the figure and shows compatibility. 0 The central values ​​(δdm, δpm, δhm) of the obtained Hansen sphere S become the HSP values ​​of the evaluation sample. The HSP value of the above pure substance used to calculate the Hansen sphere is, for example, a dispersion force term δd of 10 to 25 MPa. 1 / 2The dipole-dipole force term δp is 0 to 20 MPa. 1 / 2 The hydrogen bond term δh is about 0 to 20 MPa. 1 / 2 That's about it. In addition, since solubility depends on temperature, when determining the Hansen ball, it is preferable to carry out the solubility test at a temperature at which the resin actually dissolves.

[0054] Next, Figure 5 is a schematic diagram showing the distance between the solubility parameters of two substances, substance 1 and substance 2. First, the Hansen spheres of substance 1 and substance 2 are obtained using the method described above. The HSP value of substance 1 is (δd 1 , δp 1 , δh 1 ) and the HSP value of substance 2 is (δd 2 , δp 2 , δh 2 ), the HSP value distance between two substances (hereinafter simply referred to as “Ra”) can be calculated by the following formula 1. Ra = {4 × (δd 1 -δd 2 ) 2 +(δp 1 -δp 2 ) 2 +(δh 1 -δh 2 ) 2} 0.5 formula 1

[0055] The relative energy difference (hereinafter, simply referred to as "RED") based on the Hansen solubility parameter of substance 1 to substance 2 is expressed as follows: 0 Then, it can be calculated using the following formula 2. RED=Ra / R 0 formula 2

[0056] FIG. 6 is a schematic diagram showing a case where the RED based on the Hansen solubility parameter of substance 1 for substance 2 is within 1. In this case, as shown in FIG. 6, the HSP value of substance 1 (δd 1 , δp 1 , δh 1 ) will be located inside the Hansen sphere S2 of substance 2 (including the surface of the sphere).

[0057] FIG. 7 is a schematic diagram showing a case where the RED based on the Hansen solubility parameter of substance 1 in substance 2 is greater than 1. In this case, as shown in FIG. 7, the HSP value (δd 1 , δp 1 , δh 1 ) will be located outside S2 of the Hansen sphere of substance 2 (not including the surface of the sphere).

[0058] In the resin solution production process of the present embodiment, a resin solution is produced from a mixture containing a plurality of types of resin by not dissolving a specific resin but dissolving resins other than the specific resin. The specific resin may be one or more kinds. The resin other than the specific resin may be one or more kinds. Hereinafter, the specific resin will be referred to as “resin A,” and any resin other than the specific resin will be referred to as “resin B.” In this embodiment, from a mixture containing resin A and resin B, only resin B is dissolved.

[0059] How to select a solvent Resin A is Resin P A1 ~P Ax Resin B is made of Resin P B1 ~P By x represents the number of types of resins constituting Resin A and is an integer of 1 or more. y represents the number of types of resins constituting Resin B and is an integer of 1 or more. The value of x is not particularly limited, but from the viewpoint of facilitating the selection of the solvent, it is preferably 1 to 3, and more preferably 1 to 2. The value of y is not particularly limited, but from the viewpoint of facilitating the selection of the solvent, it is preferably 1 to 5, and more preferably 1 to 3. The value of x+y is not particularly limited, but from the viewpoint of facilitating the selection of the solvent, it is preferably 2 to 8, and more preferably 2 to 5.

[0060] By the above-mentioned method, resin P A1 ~P Ax Hansen Ball S (P A1 )~S(P Ax ) are calculated for each of the Hansen spheres S(PA1 )~S(P Ax ) from resin P A1 ~P Ax HSP value [δd(P A1 ), δp(P A1 ), δh(P A1 )]~[δd(P Ax ), δp(P Ax ), δh(P Ax )] and the interaction radius R 0 (P A1 )~R 0 (P Ax ) respectively. Similarly, P B1 ~P By Hansen Ball S (P B1 )~S(P By ) are calculated for each of the Hansen spheres S(P B1 )~S(P By ) from resin P B1 ~P By HSP value [δd(P B1 ), δp(P B1 ), δh(P B1 )]~[δd(P By ), δp(P By ), δh(P By )] and the interaction radius R 0 (P B1 )~R 0 (P By ) respectively.

[0061] The HSP values ​​of the selected solvent L are assumed to be [δd(L), δp(L), δh(L)]. Resin P A1 ~P Ax HSP value [δd(P A1 ), δp(P A1 ), δh(P A1 )]~[δd(P Ax ), δp(P Ax ), δh(P Ax )] in the above formula 1 (δd 2 , δp 2 , δh 2 ) and the HSP value of the solvent L [δd(L), δp(L), δh(L)] is calculated by (δd 1 , δp1 , δh 1 ) and Ra(P A1 )~Ra(P Ax ) are calculated respectively. A1 )~Ra(P Ax ) is a function of δd(L), δp(L), and δh(L). And, P A1 ~P Ax The interaction radius R 0 (P A1 )~R 0 (P Ax ) and the obtained Ra(P A1 )~Ra(P Ax ) into the above formula 2, and RED(P A1 )~RED(P Ax ) is calculated. The obtained RED(P A1 )~RED(P Ax ) is a function of δd(L), δp(L), and δh(L).

[0062] Similarly, Resin P B1 ~P By HSP value [δd(P B1 ), δp(P B1 ), δh(P B1 )]~[δd(P By ), δp(P By ), δh(P By )] in the above formula 1 (δd 2 , δp 2 , δh 2 ) and the HSP value of the solvent L [δd(L), δp(L), δh(L)] is calculated by (δd 1 , δp 1 , δh 1 ) and Ra(P B1 )~Ra(P By ) are calculated respectively. B1 )~Ra(P By ) is a function of δd(L), δp(L), and δh(L). And, P B1 ~P By The interaction radius R 0 (P B1 )~R 0 (P By ) and the obtained Ra(P B1)~Ra(P By ) into the above formula 2, and RED(P B1 )~RED(P By ) is calculated. The obtained RED(P B1 )~RED(P By ) is a function of δd(L), δp(L), and δh(L).

[0063] In this embodiment, RED(P A1 )~RED(P Ax ) are greater than 1 and RED(P B1 )~RED(P By ) is less than or equal to 1. Figure 8 shows the HSP value of solvent L when x is 2 and y is 2, and the HSP value of resin P A1 , P A2 Hansen Ball S (P A1 ), S(P A2 ) and Resin P B1 , P B2 Hansen Ball S (P B1 ), S(P B2 8, the HSP value [δd(L), δp(L), δh(L)] of the solvent L is A1 , P A2 Hansen Ball S (P A1 ), S(P A2 ) outside (excluding the surface of the sphere) and resin P B1 , P B2 Hansen Ball S (P B1 ), S(P B2 ) (including the surface of the sphere).

[0064] In this embodiment, RED(P A1 )~RED(P Ax ) are all greater than 1, preferably 2.5 or greater, and more preferably 3 or greater. A1 )~RED(P Ax ) is greater than (or equal to) the lower limit, resin P constituting resin A is A1 ~P Ax The dissolution of RED(PA1 )~RED(P Ax ) is not particularly limited, but is, for example, 10 or less.

[0065] In this embodiment, RED(P B1 )~RED(P By ) are all equal to or less than 1, preferably equal to or less than 0.9, and more preferably equal to or less than 0.8. B1 )~RED(P By ) is not more than the upper limit, the resin P constituting the resin B B1 ~P By The dissolution of RED(P B1 )~RED(P By The lower limit of ) is not particularly limited, but is, for example, 0.1 or more.

[0066] HSP value of solvent L and resin P A1 ~P Ax The distance between each HSP value is Ra(P A1 )~Ra(P Ax ) is RED(P A1 )~RED(P Ax ) is not particularly limited as long as it is greater than 1, but for example, 5 MPa 1 / 2 More than 10MPa is preferable. 1 / 2 The above is more preferable.

[0067] HSP value of solvent L and resin P B1 ~P By The distance between each HSP value is Ra(P B1 )~Ra(P By ) is RED(P B1 )~RED(P By ) is not particularly limited as long as it is 1 or less, but for example, 8 MPa 1 / 2 Less than 5MPa is preferable. 1 / 2 The following is more preferred:

[0068] RED(P B1 )~RED(P ByIn order to select a solvent L having an HSP value [δd(L), δp(L), δh(L)] such that all of the above are 1 or less, when y is 2 or more, B1 ~P By Hansen Ball S (P B1 )~S(P By ) all have overlapping portions. That is, resin P with y=c and y=d is randomly selected from resin B. Bc , P Bd When you select P Bc HSP value [δd(P Bc ), δp(P Bc ), δh(P Bc )] and P Bd HSP value [δd(P Bd ), δp(P Bd ), δh(P Bd )] in the above formula 1 (δd 1 , δp 1 , δh 1 ) and (δd 2 , δp 2 , δh 2 ) and substitute each of them into Ra(P Bc -P Bd ) and P Bc The interaction radius R 0 (P Bc ) and P Bd The interaction radius R 0 (P Bd ) satisfies the following formula 3. {R 0 (P Bc )+R 0 (P Bd )}≧Ra(P Bc -P Bd ) Equation 3

[0069] Resin P that does not satisfy formula 3 B1 ~P By In this case, the resin B may be appropriately selected. B1 ~P By An arbitrary resin is removed from the above so as to satisfy the formula 3. In this case, the removed resin constitutes resin A.

[0070] Resin The type of resin contained in the mixture of the present embodiment is not particularly limited, and examples thereof include polyolefin resins such as polyethylene, polypropylene, polybutadiene, and polymethylpentene; vinyl resins such as polyvinyl chloride, polyvinylidene chloride, polyvinyl alcohol, ethylene-vinyl acetate copolymer, and ethylene-vinyl alcohol copolymer; polystyrene resins such as polystyrene, acrylonitrile-styrene resin, and acrylonitrile-butadiene-styrene resin; polyester resins such as polyethylene terephthalate, polybutylene terephthalate, polyethylene naphthalate, and polytrimethylene terephthalate; and polyvinyl triacetate. Examples of suitable resins include: cellulose; polycarbonate; urethane resins such as polyurethane and acrylic-modified polyurethane; polymethylpentene; polysulfone resins such as polyethersulfone, polyphenylsulfone, and polysulfone; polyetheretherketones such as polyetherketone, polyetheretherketone, and polyetherketoneketone; polyphenylene sulfide; polyimide-based resins such as polyetherimide and polyimide; polyamide-based resins such as polyamide 6, polyamide 66, and polyamide 11; acrylic resins; fluorine-based resins; phenolic resins; epoxy resins; melamine resins; urea resins; unsaturated polyester resins; alkyd resins, etc. The mass average molecular weight of the resin contained in the mixture of this embodiment is not particularly limited as long as the effects of the present invention can be obtained, but may be, for example, 10,000 to 100,000 or 100,000 to 1,000,000.

[0071] The resin of this embodiment is solid at 30° C. or less. The form of the resin is not particularly limited as long as the effects of the present invention can be obtained, but examples include a molded body molded into a package such as a PET bottle, a pellet form, a flake form, etc. The size of the resin is not particularly limited as long as the effects of the present invention can be obtained, but the major axis is about 1 to 100 mm. From these resins, resin A and resin B can be arbitrarily selected according to the application described below.

[0072] Solvent The solvent in this embodiment is RED(P A1 )~RED(P Ax ) are greater than 1 and RED(P B1 )~RED(P By) has an HSP value of 1 or less. Examples of the solvent include esters such as methyl formate, ethyl formate, propyl formate, pentyl formate, methyl acetate, ethyl acetate, pentyl acetate, benzyl acetate, benzyl benzoate, ethyl benzoate, and butyl benzoate; ketones such as acetone, diisobutyl ketone, ethyl methyl ketone, cyclopentanone, cyclohexanone, methylcyclohexanone, γ-butyrolactone, and N-methyl-2-pyrrolidone; diethyl ether, methyl tert-butyl ether, diisopropyl ether, dimethoxymethane, and dimethoxyethane. Ethers such as 1,4-dioxane, 1,3-dioxolane, 4-methyldioxolane, tetrahydrofuran, methyltetrahydrofuran, anisole, phenetole, and 2-methoxytetrahydropyran; methanol, ethanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, tert-butanol, 1-pentanol, 2-methyl-2-butanol, methoxypropanol, diacetone alcohol, cyclohexanol, 2-fluoroethanol, and 2,2,2-trifluoroethane. Examples of the organic solvent include alcohols such as ethanol and 2,2,3,3-tetrafluoro-1-propanol; glycol ethers such as ethylene glycol monomethyl ether, ethylene glycol monoethyl ether, ethylene glycol monobutyl ether, ethylene glycol monoethyl ether acetate, and triethylene glycol dimethyl ether; organic solvents having an amide group such as N,N-dimethylformamide, acetamide, and N,N-dimethylacetamide; organic solvents having a nitrile group such as acetonitrile, isobutyronitrile, propionitrile, and methoxyacetonitrile; organic solvents having a carbonate group such as ethylene carbonate, propylene carbonate, and 1,2-glycerol carbonate; halogenated hydrocarbons such as methylene chloride, chloroform, tetrachloroethane, and chlorobenzene; and hydrocarbons such as n-pentane, cyclohexane, n-hexane, 1-octadecene, benzene, toluene, xylene, 2,2,4-trimethylpentane, cyclohexene, ethylbenzene, d-limonene, and l-limonene.

[0073] The solvent may be used alone or in combination of two or more kinds. That is, the solvent of the present embodiment may be a mixture of two or more kinds of solvents (hereinafter, also referred to as a "mixed solvent"). Examples of the mixed solvent include a mixture of two or more kinds of the solvents listed above.

[0074] Other mixed solvents include petroleum fractions obtained in the refining process of crude oil, such as atmospheric residual oil, vacuum gas oil, vacuum residual oil, desulfurized atmospheric residual oil, desulfurized vacuum gas oil, light cracked gas oil, and heavy cracked gas oil; vegetable oils, such as soybean oil, rapeseed oil, sunflower oil, corn oil, cottonseed oil, peanut oil, olive oil, palm oil, sesame oil, rice oil, and orange oil, and waste oils thereof. The above-mentioned solvents may also be mixed into these mixed solvents.

[0075] When a mixed solvent is used as the solvent in this embodiment, the HSP value of the mixed solvent may be determined by the method described above, or may be determined as a weighted average of the HSP values ​​of the solvents constituting the mixed solvent as described below. Mixed solvent L is solvent L 1 ~L z The ratio of the volume of the solvent L to the total volume of all the solvents before mixing in the mixed solvent 1 ~L z The content ratio of each is V(L 1 )~V(L z ) Solvent L 1 ~L z The HSP values ​​of [δd(L 1 ), δp(L 1 ), δh(L 1 )]~[δd(L z ), δp(L z ), δh(L z )], then the HSP values ​​of the mixed solvent, [Δd(L), Δp(L), Δh(L)], can be calculated by the following formulas 4 to 6.

[0076]

number

[0077]

number

[0078]

number

[0079] In this embodiment, the HSP value of the mixed solvent is preferably determined by the above formulas 4 to 6.

[0080] The boiling point of the solvent in this embodiment is not particularly limited as long as the effects of the present invention can be obtained, but may be, for example, 80 to 700°C, 150 to 500°C, or 200 to 400°C. The density of the solvent in this embodiment is not particularly limited as long as the effects of the present invention can be obtained, but is, for example, 0.70 to 1.5 g / cm 3 Also, 0.80 to 1.2 g / cm 3 Also, 0.85 to 1.2 g / cm 3 That's fine too.

[0081] 〇Combination of Resin A, Resin B and Solvent L In this embodiment, it is preferable that resin A contains a chlorine element. Also, in this embodiment, it is preferable that resin B and solvent L do not contain a chlorine element. When the raw oil containing the resin solution obtained in the resin dissolving step of this embodiment is treated in an oil refinery, if the resin solution contains a chlorine element, hydrogen chloride may be generated during the treatment process in the oil refinery, which may corrode the oil refinery. Since resin A contains a chlorine element and resin B and solvent L do not contain a chlorine element, the resulting solution does not contain a chlorine element, making it possible to prevent corrosion of the oil refinery. The resin contained in the mixture of the present embodiment is preferably at least one resin selected from the group consisting of polyethylene, polypropylene, polystyrene, and polyvinyl chloride.

[0082] When the resins constituting resin A are polystyrene or polyvinyl chloride, and the resins constituting resin B are polyethylene or polypropylene, examples of solvents that have a relative energy difference based on the Hansen solubility parameters with respect to resin A of more than 1 and a relative energy difference based on the Hansen solubility parameters with respect to resin B of 1 or less include benzene, cyclohexane, and ethylbenzene.

[0083] When the resins constituting resin A are polypropylene and polyvinyl chloride, and the resins constituting resin B are polyethylene and polystyrene, examples of solvents that have a relative energy difference based on the Hansen solubility parameters with respect to resin A of more than 1 and a relative energy difference based on the Hansen solubility parameters with respect to resin B of 1 or less include butyl benzoate, benzyl acetate, and orange oil.

[0084] When the resins constituting resin A are polyethylene and polyvinyl chloride, and the resins constituting resin B are polypropylene and polystyrene, an example of a solvent that has a relative energy difference based on the Hansen solubility parameters with respect to resin A of more than 1 and a relative energy difference based on the Hansen solubility parameters with respect to resin B of 1 or less is chlorobenzene.

[0085] When the resins constituting resin A are polyethylene and polypropylene, and the resins constituting resin B are polystyrene and polyvinyl chloride, examples of solvents that have a relative energy difference based on the Hansen solubility parameters with respect to resin A of more than 1 and a relative energy difference based on the Hansen solubility parameters with respect to resin B of 1 or less include N-methylpyrrolidone and N,N-dimethylacetamide.

[0086] When the resin constituting resin A is polypropylene and the resin constituting resin B is polyethylene, polystyrene, or polyvinyl chloride, examples of a solvent having a relative energy difference based on the Hansen solubility parameters of more than 1 with respect to resin A and a relative energy difference based on the Hansen solubility parameters of 1 or less with respect to resin B include a mixed solvent of ethyl benzoate, 2-methoxytetrahydropyran, 81% by mass of d-limonene and 19% by mass of 1,2-glycerol carbonate, a mixed solvent of 64% by mass of d-limonene and 36% by mass of dimethylformamide, a mixed solvent of 58% by mass of tetrahydrofuran and 42% by mass of cyclohexanone, a mixed solvent of 62% by mass of ethyl acetate and 38% by mass of benzyl benzoate, and a mixed solvent of 58% by mass of methyl ethyl ketone and 42% by mass of benzyl benzoate.

[0087] When the resin constituting resin A is polyvinyl chloride and the resin constituting resin B is polyethylene, polypropylene, or polystyrene, examples of solvents that have a relative energy difference based on the Hansen solubility parameters with respect to resin A of more than 1 and a relative energy difference based on the Hansen solubility parameters with respect to resin B of 1 or less include 1,1,1,2-tetrachloroethane, d-limonene, o-xylene, toluene, etc.

[0088] (Conditions for dissolving resin) In the method for dissolving a resin of this embodiment, the ratio of the mixture to the total mass of the solvent is not particularly limited as long as it is capable of dissolving resin B, but may be, for example, 1 to 50 mass %, 1 to 40 mass %, or 1 to 30 mass %. In the method for dissolving a resin of this embodiment, the ratio of resin B to the total mass of the solvent is not particularly limited as long as resin B can be dissolved in the solvent, but may be, for example, 1 to 20 mass%, 1 to 18 mass%, or 1 to 15 mass%. The temperature at which resin B is dissolved is not particularly limited as long as resin B can be dissolved; however, the temperature may be 15 to 100°C, 20 to 90°C, or 30 to 80°C, as long as resin A does not soften or melt. When dissolving Resin B, it is preferable to carry out stirring, ultrasonic treatment, or the like.

[0089] In the method for dissolving a resin according to the present embodiment, it is preferable that the entire resin B is dissolved, but 80 to 100 mass % or 90 to 100 mass % of the total mass of resin B may be dissolved. In the method for dissolving a resin of this embodiment, it is preferable that resin A is not dissolved, but resin A may be dissolved in an amount of 0 mass % or more and less than 1 mass %, or 0 to 0.5 mass %, relative to the total mass of resin A.

[0090] For example, if the resin contains a heteroatom such as a halogen element, the amount of the resin dissolved can be confirmed by measuring the content of the heteroatom in the solution. The amount of the resin dissolved that does not contain a heteroatom can be measured by a conventionally known analysis method, and examples of the analysis method include infrared spectroscopy, gas chromatography mass spectrometry, and gel filtration permeation chromatography.

[0091] <Fluid catalytic cracking reaction process> In the process of treating the feedstock oil containing the resin solution in the FCC facility of this embodiment, the feedstock oil containing the resin solution produced in the above-mentioned resin solution production process is treated in the FCC facility. Specifically, the feedstock oil containing the resin solution is supplied to the FCC facility and contacted with the FCC catalyst to carry out a fluid catalytic cracking reaction and produce a cracked oil containing petroleum products.

[0092] In this embodiment, the fluid catalytic cracking reaction can be carried out by a method known in the art. The fluid catalytic cracking reaction can be carried out in an FCC facility by contacting a feedstock oil containing a resin solution with an FCC catalyst at a high temperature.

[0093] In this embodiment, the feedstock oil to be cracked contains a resin solution. Only the resin solution may be used as the feedstock oil, or the resin solution may be mixed with a fluid catalytic cracking feedstock oil to obtain the feedstock oil. The fluid catalytic cracking feedstock oil to be mixed with the resin solution is not particularly limited, and examples thereof include hydrocarbon oils (hydrocarbon mixtures) that are liquid at normal temperature and pressure.

[0094] Examples of the hydrocarbon oil include one or more selected from light oil fractions obtained by atmospheric or reduced pressure distillation of crude oil, atmospheric distillation residual oils, and reduced pressure distillation residual oils, and also include one or more selected from coker light oil, solvent deasphalted oil, solvent deasphalted asphalt, tar sands oil, shale oil, coal liquefied oil, GTL (Gas to Liquids) oil, vegetable oil, waste lubricating oil, waste edible oil, etc.

[0095] Furthermore, the fluid catalytic cracking feedstock oil used in the present embodiment may also include hydrotreated oil obtained by subjecting the above-mentioned hydrocarbon oil to hydrotreatment well known to those skilled in the art, i.e., hydrodesulfurization under high temperature and pressure in the presence of a hydrotreatment catalyst such as a Ni-Mo based catalyst, a Co-Mo based catalyst, a Ni-Co-Mo based catalyst, or a Ni-W based catalyst.

[0096] The fluid catalytic cracking reaction of the feedstock oil in this embodiment can be carried out by continuously circulating an FCC catalyst in an FCC facility 1, which is usually composed of a vertically installed riser 10, a reaction tower 20, and a regenerator 30. In this specification, the fluid catalytic cracking facility (FCC facility) also includes a residual oil fluid catalytic cracking facility (RFCC facility). That is, in this specification, the fluid catalytic cracking reaction also includes a residual oil fluid catalytic cracking reaction.

[0097] The fluid catalytic cracking reaction carried out by the FCC facility will now be described in detail. A pumping fluid flows upward in the riser 10, and the FCC catalyst supplied from the regenerated catalyst transfer line 34 flows upward in the riser 10 together with the pumping fluid. The resin solution is heated to a predetermined temperature by the preheating device 52, steam is added, and then the resin solution is supplied to the riser 10 from the resin solution supply line 51. Similarly, fluid catalytic cracking feedstock may be heated to a predetermined temperature by the preheating device 12 and supplied to the riser 10 from the fluid catalytic cracking feedstock supply line 11. The feedstock containing the resin solution supplied to the riser 10 comes into contact with the FCC catalyst, and a cracking reaction occurs. The cracked oil and the FCC catalyst produced by the cracking reaction are transferred to the reaction tower 20. The concentration of the resin relative to the total mass of the resin solution supplied is not particularly limited as long as the effects of the present invention can be obtained, but may be, for example, 1 to 50 mass%, 5 to 40 mass%, or 5 to 30 mass%.

[0098] As the operating conditions of the riser 10, the reaction temperature is preferably 490 to 530°C, and more preferably 500 to 520°C. When the reaction temperature in the riser 10 is equal to or higher than the lower limit of the above range, the cracking reaction of the feed oil containing the resin solution proceeds, and the yield of petroleum products is improved. When the reaction temperature in the riser 10 is equal to or lower than the upper limit of the above range, the amount of light gas such as dry gas produced by thermal cracking and the amount of coke produced can be reduced, and the yield of petroleum products can be relatively easily increased, which is economical.

[0099] The reaction pressure is from normal pressure to 0.49MPa (5kg / cm 2 ), and normal pressure to 0.29 MPa (3 kg / cm 2 Since the decomposition reaction is a reaction in which the number of moles of the product increases relative to the number of moles of the reactants, it is thermodynamically (equilibrium-wise) advantageous for the reaction pressure in the riser 10 to be 0.49 MPa or less.

[0100] The mass ratio of FCC catalyst / feed oil is preferably 3 to 7, and more preferably 4 to 6. When the mass ratio of FCC catalyst / feed oil in the riser 10 is equal to or higher than the lower limit of the above range, the catalyst concentration in the riser 10 can be kept at an appropriate level, and the efficiency of cracking the feed oil is improved. Even when the mass ratio of FCC catalyst / feed oil in the riser 10 is equal to or lower than the upper limit of the above range, the cracking reaction of the feed oil proceeds effectively, and it becomes easier to proceed with the cracking reaction commensurate with the increase in the catalyst concentration.

[0101] The ratio of the flow rate (KL / H) of the resin dissolved solution to the total flow rate [KL / H] of the resin dissolved solution supplied from the resin dissolved solution supply line 51 and the fluid catalytic cracking feed oil supplied from the fluid catalytic cracking feed oil supply line 11 ((resin dissolved solution / (fluid catalytic cracking feed oil+resin dissolved solution))×100%) is preferably 5 to 100%, more preferably 10 to 95%, and even more preferably 20 to 80%.

[0102] The cracked oil produced by the cracking of the feed oil in the riser 10 is supplied to the cyclone 21. The cyclone 21 separates the cracked oil from the FCC catalyst by using centrifugal force. The cracked oil is then discharged from the reaction tower 20 through the cracked oil discharge line 22 and transferred to the distillation tower 41.

[0103] The FCC catalyst separated by the cyclone 21 is supplied to a stripper 23. Steam, nitrogen, etc. are supplied to the stripper 23. In the stripper 23, the hydrocarbons on the FCC catalyst are removed by the steam, nitrogen, etc. Then, the FCC catalyst is discharged from the reaction tower 20 through a post-reaction catalyst transfer line 24 and transferred to a regeneration tower 30.

[0104] The temperature during the stripping treatment in the stripper 23 is usually 470 to 530° C., preferably 480 to 520° C., and more preferably 490 to 510° C. As the gas used for stripping, steam generated by a boiler, an inert gas such as nitrogen pressurized by a compressor, etc., and the like are used.

[0105] Air is supplied from an air blower 31 to an air grid 32, and then from the air grid 32 into the regenerator 30, whereby the coke on the FCC catalyst after stripping transferred to the regenerator 30 is burned, and the FCC catalyst is regenerated. The regenerated FCC catalyst and the exhaust gas generated by the combustion of the coke are separated by a cyclone 33. The regenerated FCC catalyst is discharged from the regenerator 30 through a regenerated catalyst transfer line 34 and supplied to the riser 10. The exhaust gas is discharged from the regenerator 30 through an exhaust gas line 35.

[0106] As for the operating conditions of the catalyst regenerator, the regeneration temperature is preferably 600 to 800°C, and more preferably 700 to 750°C. If the regeneration temperature in the catalyst regeneration tower is 600°C or higher, the coke is burned sufficiently and the catalyst activity is sufficiently restored. Also, if the regeneration temperature in the catalyst regeneration tower is 800°C or lower, the adverse effect on the equipment material is low.

[0107] The cracked oil is transferred from the reaction tower 20 to the distillation tower 41 via the cracked oil discharge line 22, and in the distillation tower 41, a fraction containing compounds having about 1 to 13 carbon atoms is distilled from the top of the tower, heavy cracked gas oil (HCO) and light cracked gas oil (LCO) are distilled from the middle of the tower, and fluid catalytic cracking residual oil (SLO) is distilled from the bottom of the tower, thereby producing petroleum products.

[0108] The fraction containing compounds having carbon numbers of about 1 to 13 is transferred from distillation column 41 to distillation column 43 via line 42, in which gas components are removed from the top of distillation column 43, and a fraction mainly composed of liquefied petroleum gas (LPG) and gasoline is obtained at the bottom of the column. The fraction mainly composed of LPG and gasoline is transferred from distillation tower 43 to distillation tower 45 via line 44, and in distillation tower 45, the fraction mainly composed of LPG is distilled from the top of the tower, and the fraction mainly composed of gasoline is obtained from the bottom of the tower. The fraction mainly composed of LPG is transferred from distillation column 45 to distillation column 47 via line 46. In distillation column 47, a fraction mainly composed of propylene, a petrochemical feedstock, is distilled from the top of the column, and a fraction mainly composed of butene, a petrochemical feedstock, is obtained from the bottom of the column. The fraction mainly composed of gasoline is transferred from the distillation tower 45 via line 48 to the aromatics extraction unit 60, where it is separated into a fraction mainly composed of aromatic compounds, which are petrochemical feedstocks, and a fraction mainly composed of gasoline from which the aromatic compounds have been removed. The fraction containing mainly gasoline from which the aromatic compounds have been removed is transferred via line 61 to a naphtha cracker 70, which produces a fraction containing mainly the petrochemical raw materials ethylene, propylene, and aromatic compounds. In addition, the fraction mainly composed of gasoline from which the aromatic compounds have been removed is transferred via line 62 to a catalytic reformer 80, which produces a fraction mainly composed of aromatic compounds, which are petrochemical feedstocks.

[0109] <Petrochemical raw materials> Examples of the petrochemical raw materials produced by the method for producing a petrochemical raw material of this embodiment include olefins having 3 to 8 carbon atoms, aromatic compounds, etc. Examples of the olefins having 3 to 8 carbon atoms include propylene, 1-butene, 2-butene, isobutene, 1,3-butadiene, etc. Examples of the aromatic compounds include benzene, toluene, o-xylene, m-xylene, p-xylene, ethylbenzene, etc.

[0110] <Process for obtaining energy from waste> In this embodiment, the energy required in the process of processing raw oil in an oil refinery facility is energy obtained by burning either or both of combustible materials including waste and methane obtained from the waste. The waste is preferably municipal waste.

[0111] Combustible materials, including waste, include waste plastics, food waste such as food residues and garbage, and other combustible waste (hereinafter, other combustible waste will also be referred to as "combustible waste"). It is preferable that the above three types are separated in advance.

[0112] The production of waste-derived energy in the combustion equipment 102 and the power generation equipment 104 will be described using an example in which the combustion equipment 102 is the above-mentioned combustion equipment equipped with a garbage pit, a crane, an incinerator, a waste heat boiler, an economizer, an ash pit, a dust collector, and a denitrification reaction tower, and the power generation equipment 104 is a turbine-type power generation equipment.

[0113] Combustible waste is dumped into a garbage pit and stored there. The combustible materials stored in the garbage pit are dumped into an incinerator by a crane or the like. The combustible materials are incinerated in the incinerator, and the heat of the exhaust gas generated by the incineration is recovered by a waste heat boiler and an economizer. The incineration of the combustible materials may be performed using methane supplied to the combustion equipment 102 via a methane supply line L302 as fuel, as necessary. The economizer preheats the feedwater, and steam is produced in the waste heat boiler. The produced steam is supplied to the oil refinery equipment 101 via a steam supply line L201. Furthermore, the produced steam is supplied to the power generation equipment 104 via a steam supply line L204. The ash from the incinerator is sent to an ash pit and then removed. The temperature of the exhaust gas generated by incineration is lowered by the waste heat boiler and economizer, and then the gas is released into the atmosphere after removing harmful substances in a dust collector and a denitrification tower.

[0114] In the power generation facility 104, power is generated by the steam supplied via the steam supply line L204. The generated power is supplied to the oil refinery facility 101 via the power supply line L401.

[0115] When burning waste to produce steam and generating electricity using the produced steam, the amount of steam produced and the power output are unstable due to partial or complete shutdown of the incineration plant for periodic inspection and repair, fluctuations in the amount of incineration, fluctuations in the quality of the waste, etc., so there is a problem that it is difficult to use energy efficiently. In this embodiment, the steam produced by the incineration plant 102 and the power generated by the power generation plant 104 are used in the process of treating raw oil in an oil refinery. In the oil refinery, a huge amount of energy is used while being precisely controlled. That is, in the oil refinery, the energy produced by the existing boiler and power generation plant is used in combination with the energy derived from the waste of this embodiment. Therefore, in this embodiment, even if there is a fluctuation in the amount of steam produced by the combustion plant 102 and the power output of the power generation plant 104, the fluctuation can be sufficiently stabilized by adjusting the amount of energy produced by the existing boiler and power generation plant, and the power can be used efficiently.

[0116] The production of energy derived from waste in the microbial fermentation facility 103 will be described below by taking as an example the case where the microbial fermentation facility 103 is the above-mentioned microbial treatment facility equipped with a separator, a slurry tank, a methane fermenter, and a desulfurization tower.

[0117] First, a separator removes contaminants such as plastic bags and plastics from food waste. The food waste after removal is transferred to a slurry tank, and water is added to make a slurry. The slurry is transferred to a methane fermentation tank, and the organic matter contained in the slurry is converted into biogas mainly composed of methane gas and carbon dioxide by methane fermentation bacteria. The resulting biogas is transferred to a desulfurization tower, where hydrogen sulfide is removed and biogas containing methane gas is produced. The produced biogas containing methane gas is supplied to an oil refinery facility 101 via a methane supply line L301. The produced biogas containing methane gas is further supplied to a combustion facility 102 via a methane supply line L302.

[0118] The steam supplied to the oil refinery 101 via the steam supply line L201 is used as power for pumps used in the oil refinery 101, a reboiler for the distillation tower, and the like. Furthermore, when the oil refinery is an FCC facility, the steam is used as steam for circulating the catalyst, steam for dispersing the feed oil, steam for separating the catalyst and cracked oil after the reaction in the reaction tower 20, and steam used in the stripper 23. Furthermore, when the oil refinery 101 is equipped with a dissolving tank 50, the steam is used to heat the dissolving tank.

[0119] The methane supplied to the oil refinery 101 via the methane supply line L301 is used as a raw material for heating the heating furnace (including the preheater) of the oil refinery 101. In addition, if the generated methane is in excess, it is used, for example, as a raw material for a hydrogen production device.

[0120] The electric power supplied to the oil refinery 101 via the electric power supply line L401 is used for devices that use electric power in the oil refinery 101. Furthermore, in the case where the oil refinery 101 is equipped with a dissolution tank 50, the electric power is used to power the agitator of the dissolution tank and a transport pump for transporting the resin solution from the dissolution tank 50 to the riser 10.

[0121] When the amount of waste is small compared to the steam and electricity required for the oil refinery 101, steam and electricity may be supplied to the oil refinery from a boiler and power generation facility that uses normal fossil fuels. Also, fossil fuels may be used as auxiliary fuel for the combustion facility 102.

[0122] It is preferable that the oil refining equipment 101, the combustion equipment 102, the microbial treatment equipment 103, and the power generation equipment 104 are installed geographically in close proximity to each other, and the distance between each equipment is preferably 0.1 to 5 km, and more preferably 0.1 to 1 km. Usually, an oil refining facility is located within an oil refinery facility. Since the oil refinery facility has a plurality of high-pressure gas facilities, it is preferable that the combustion facility 102 is installed outside the oil refinery facility. In other words, it is preferable that the combustion of either or both of the combustible materials including waste and the methane obtained from the waste is performed outside the oil refinery facility.

[0123] The amount of steam produced by the combustion equipment 102 is preferably 5,000 to 20,000 tons / day, and more preferably 10,000 to 15,000 tons / day. The ratio of the amount of steam produced in one day by the combustion equipment 102 to the amount of steam required in one day in the process of processing the above-mentioned raw material oil in the oil refining equipment is preferably 1 to 120%, and more preferably 1 to 100%. When the ratio is equal to or greater than the lower limit of the range, consumption of fossil fuels can be reduced accordingly.

[0124] The amount of electric power generated by the power generation facility 104 is preferably 500,000 to 2,000,000 kWh / day, and more preferably 800,000 to 1,500,000 kWh / day. The ratio of the amount of electricity generated in one day by the power facility 104 to the amount of electricity required in one day in the process of processing the above-mentioned raw oil in the oil refining facility is preferably 1 to 120%, and more preferably 1 to 100%. When the ratio is equal to or greater than the lower limit of the range, consumption of fossil fuels can be reduced accordingly. [Explanation of symbols]

[0125] 1...Fluid catalytic cracking equipment, 10...Riser, 11...Fluid catalytic cracking feed oil supply line, 12...Preheater, 20...Reaction tower, 21...Cyclone, 22...Cracked oil discharge line, 23...Stripper, 24...Post-reaction catalyst transfer line, 30...Regeneration tower, 31...Air blower, 32...Air grid, 33...Cyclone, 34...Regenerated catalyst transfer line, 35...Exhaust gas line, 40...Refining equipment, 41...Distillation tower, 42...Line, 43...Distillation tower, 44...Line, 45...Distillation tower, 46...Line, 47...Distillation tower , 48...line, 50...resin dissolution tank, 51...resin solution supply line, 52...preheating device, 60...aromatic extraction device, 61...line, 62...line, 70...naphtha cracker, 80...catalytic reforming device, 100...petroleum product manufacturing system, 101...oil refining equipment, 102...combustion equipment, 103...microbial treatment equipment, 104...power generation equipment, L201...steam supply line, L204...steam supply line, L301...methane supply line, L302...methane supply line, L401...electricity supply line

Claims

1. A method for producing a petroleum product, comprising the steps of: processing a feedstock oil in an oil refining facility to produce a petroleum product, The raw material oil includes a resin solution in which waste plastic is dissolved in a solvent, A resin solution production process is provided for obtaining a resin solution by dissolving a specific resin from the waste plastic, which is a mixture containing a plurality of types of resin, without dissolving a specific resin, and dissolving resins other than the specific resin, A method for producing a petroleum product, in which the energy required for the treatment is obtained by burning either or both of combustible materials including waste and methane obtained from the waste.

2. 2. The method for producing a petroleum product according to claim 1, wherein a solvent for dissolving is selected that has a relative energy difference based on the Hansen solubility parameter for the specific resin of more than 1 and a relative energy difference based on the Hansen solubility parameter for resins other than the specific resin of 1 or less.

3. The method for producing a petroleum product according to claim 1 or 2, wherein the feedstock oil contains a resin derived from waste plastic.

4. The method for producing a petroleum product according to any one of claims 1 to 3, wherein combustion of either or both of the combustible material containing waste and the methane obtained from the waste is carried out outside an oil refinery facility.

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