Bitumen partial modification method and thermal cracking mixture produced thereby

Abstract

The present invention relates to: a method for partially modifying bitumen; and a thermal cracking mixture produced thereby. Specifically, the present invention aims to provide a thermal cracking mixture containing a certain amount of moisture, wherein the thermal cracking mixture is obtained by thermally cracking the bitumen or bitumen-derived distillation residue with water vapor through a thermal cracking process. The thermal cracking mixture has greatly improved fluidity, thereby significantly reducing the amount of a diluent having been essentially used in existing bitumen transport methods, and in some cases, enables bitumen to be transported in a pipeline without a diluent. The thermal cracking process is performed with a reactor having a bubble column, and water steam is injected through the bubble column to react with raw materials, thereby enabling efficient partial modification even at a low temperature and pressure as compared to existing thermal cracking processes, and effectively reducing the density and viscosity of a thermal cracking mixture.

Description

Bitumen partial reforming method and pyrolysis mixture produced thereby

[0001] The present invention relates to a method for partially reforming bitumen and a pyrolysis mixture produced therefrom.

[0002] Bitumen is composed of extremely heavy and complex hydrocarbons, with distillate residues and asphaltenes being the primary contributors to its density and viscosity. These components reduce bitumen flowability, reducing processing efficiency. Various technologies are being developed to address this issue. One of the most recently attracting attention is the partial reforming process. This process selectively decomposes or removes asphaltenes and high molecular weight hydrocarbons within bitumen by combining relatively mild pyrolysis and solvent deasphalting. The pyrolysis process converts bitumen's complex polymer structure into lower molecular weight components, improving its properties. The solvent deasphalting process effectively separates the asphaltenes, reducing bitumen's density. This reduction in bitumen viscosity and density improves the efficiency of subsequent processing and manufacturing processes, and it also provides favorable conditions for long-distance transportation. Partial reforming not only improves bitumen properties but also offers the additional benefit of increasing light oil yield.

[0003] The present invention aims to provide a pyrolysis mixture having fluidity that facilitates pipeline transportation and an excellent partial reforming conversion rate.

[0004] Another object of the present invention is to provide a method for partially reforming bitumen for producing the pyrolysis mixture. The method for partially reforming bitumen is characterized by injecting steam together with bitumen or bitumen-derived distillation residue during the pyrolysis process and allowing them to react together, and the produced pyrolysis mixture contains a certain amount of moisture and exhibits excellent fluidity, reforming efficiency, and conversion rate.

[0005] The present invention is a thermal cracking mixture manufactured by mixing bitumen or bitumen-derived distillation residue and steam and thermally cracking it.

[0006] The above pyrolysis mixture provides a pyrolysis mixture containing moisture of 20 wt% or less.

[0007] In one embodiment, the pyrolysis mixture may contain 0 to 15 wt% of moisture.

[0008] In one embodiment, the pyrolysis mixture may be one in which more than 20% of the mass of bitumen or bitumen-derived distillation residue is converted into a mixture of hydrocarbon gas, naphtha, middle distillates, and gas oil.

[0009] In one embodiment, the bitumen-derived pyrolysis mixture for transportation may include 0.05 to 5 parts by weight of hydrocarbon gas, 0.1 to 10 parts by weight of naphtha, 1 to 50 parts by weight of middle distillates, and 20 to 80 parts by weight of gas oil, based on 100 parts by weight of bitumen or distillation residue obtained by distilling bitumen.

[0010] In one embodiment, the pyrolysis mixture has a kinematic viscosity of 500,000 mm at 40°C. 2 / s may be less than that.

[0011] In one embodiment, the bitumen-derived pyrolysis mixture for transportation may have a kinematic viscosity reduction of 90% or more compared to distillation residue oil.

[0012] In one embodiment, the bitumen-derived pyrolysis mixture for transportation may have an API (American Petroleum Institute) gravity of 2 to 25.

[0013] In one embodiment, the pyrolysis mixture may include a C7 asphaltene content of 25 wt% or less according to ASTM D3279.

[0014] Another aspect of the present invention is a method for partially reforming bitumen, comprising a pyrolysis process step of injecting bitumen or bitumen-derived distillation residue and steam into a pyrolysis reactor and performing a pyrolysis reaction to obtain a pyrolysis mixture;

[0015] The above thermal decomposition process step is performed in a reactor having a bubble column, and a method for partially reforming bitumen is provided in which the steam is injected into the reactor through the bubble column.

[0016] In one embodiment, the thermal cracking process step may be to inject steam into the reactor through a bubble column in an amount of 1 to 100 parts by weight based on 100 parts by weight of bitumen or bitumen-derived distillation residue oil.

[0017] In one embodiment, the thermal cracking process step may be to inject steam into the reactor through a bubble column in an amount of 1 to 100 parts by weight based on 100 parts by weight of bitumen or bitumen-derived distillation residue oil.

[0018] In one embodiment, the thermal decomposition process step may be performed under pressure conditions of 5 to 80 barg.

[0019] In one embodiment, the thermal decomposition process step may be performed at a temperature of 300 to 500°C.

[0020] In one embodiment, the thermal decomposition process step may be performed with a residence time of 5 to 250 minutes.

[0021] In one embodiment, the thermal decomposition process step may be performed by further including one or more mixed catalysts selected from the group consisting of catalysts of the aluminum silicate, zeolite, molybdenum (Mo), nickel (Ni), iron (Fe), vanadium (V), tungsten (W), manganese (Mn), copper (Cu), zinc (Zn), and cobalt (Co) series.

[0022] In one embodiment, the mixed catalyst may be included in an amount of 0.005 to 0.1 parts by weight relative to 100 parts by weight of bitumen or bitumen-derived distillation residue oil to perform a thermal decomposition process.

[0023] In one aspect, the bitumen partial modification method may further include a step of controlling the moisture content of the obtained pyrolysis mixture after the pyrolysis process step.

[0024] A pyrolysis mixture according to one embodiment of the present invention is manufactured by contacting bitumen or bitumen-derived distillation residue with steam, and contains a certain amount of moisture, thereby exhibiting excellent fluidity. The pyrolysis mixture enables pipeline transport of bitumen with a small amount of diluent or without a diluent, and can effectively address the viscosity control essential for existing bitumen transport methods. In addition, it contributes to improving physical properties by suppressing asphaltene formation in bitumen, and can promote bitumen reforming reactions.

[0025] Figure 1 shows a process diagram of one embodiment of a bitumen partial modification method according to the present invention.

[0026] Figure 2 shows a process diagram of one embodiment of a bitumen partial modification method according to the present invention.

[0027] Figure 3 shows a process diagram of one embodiment of a bitumen partial modification method according to the present invention.

[0028] Figure 4 shows a process diagram of one embodiment of a bitumen partial modification method according to the present invention.

[0029] The present invention will be described in more detail below. However, the following specific examples or examples are merely references for explaining the present invention in detail, and the present invention is not limited thereto, and may be implemented in various forms.

[0030] Additionally, unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein is for the purpose of describing specific embodiments only and is not intended to be limiting.

[0031] Additionally, the singular forms used in the specification and the appended claims are intended to include the plural forms as well, unless the context clearly dictates otherwise.

[0032] Additionally, when a part is said to "include" a component, this does not mean that it excludes other components, but rather that it may include other components, unless otherwise specifically stated.

[0033] Additionally, unless otherwise specifically defined in the present invention, when a layer or member is said to be “located on” another layer or member, this includes not only cases where a layer or member is in contact with another layer or member, but also cases where another layer or another member exists between the two layers or two members.

[0034] In addition, the terms “about,” “substantially,” etc. used in this specification are used in a meaning close to or at the numerical value when manufacturing and material tolerances inherent to the meanings mentioned are presented, and are used to prevent unscrupulous infringers from unfairly using the disclosure contents in which exact or absolute values ​​are mentioned to aid in the understanding of the present invention.

[0035] The present invention will be described below.

[0036] The present invention is a thermal cracking mixture manufactured by mixing bitumen or bitumen-derived distillation residue and steam and thermally cracking it.

[0037] The above pyrolysis mixture provides a pyrolysis mixture containing moisture of 20 wt% or less.

[0038] In one embodiment, the bitumen-derived distillation residue is a residue with a high boiling point and high molecular weight remaining after distillation in the distillation process of bitumen, and may be an atmospheric residue obtained through atmospheric distillation distillation under atmospheric pressure conditions and a vacuum residue obtained through vacuum distillation distillation under low pressure conditions (5 to 100 mmHg), but is not limited thereto as long as it is a bitumen-derived distillation residue obtained through a conventional distillation method.

[0039] In one embodiment, the pyrolysis mixture may contain moisture in an amount of 0 to 15 wt%, 5 to 15 wt%, or 10 to 15 wt%. A pyrolysis mixture containing moisture in the above content range can significantly reduce the viscosity of bitumen, thus exhibiting excellent fluidity and enabling transport without a diluent. In addition, the formation of asphaltenes in bitumen or bitumen-derived distillation residue can be prevented during the pyrolysis process, thereby achieving the object of the present invention. A pyrolysis mixture containing moisture in the above content range may be one in which vacuum residue and moisture form an emulsion such that moisture is dispersed within the oil fraction. A pyrolysis mixture produced through bitumen partial reforming according to the production method of the present invention contains moisture during the pyrolysis process, and may have a moisture content of 5 to 20 wt%, 5 to 15 wt%, or 10 to 15 wt% from the viewpoint of facilitating pipeline transport. It is preferable that the above moisture be removed after pipeline transport, and for example, moisture may be removed so that the moisture content becomes 5 wt% or less, 4 wt% or less, 3 wt% or less, 2 wt% or less, 1 wt% or less, or 0 wt%.

[0040] Excessive moisture content may alter the inherent characteristics (chemical composition, physical properties) of bitumen or bitumen-derived distillation residue, make it difficult to control viscosity, which may cause uneven fluid flow, and may make pipeline transport impossible.

[0041] In one embodiment, the pyrolysis mixture may be one in which 20 to 60%, 25 to 50%, or 30 to 45% of the mass of the distillation residue oil is converted into a high value-added mixture such as hydrocarbon gas, naphtha (IBP (Initial Boiling Point) ~ 117 ℃), middle distillates (177 to 343 ℃), and gas oil (343 to 524 ℃), but is not limited thereto.

[0042] In one embodiment, the bitumen-derived pyrolysis mixture for transportation may include 0.05 to 5 parts by weight of hydrocarbon gas, 0.1 to 10 parts by weight of naphtha, 1 to 50 parts by weight of middle distillates, and 20 to 80 parts by weight of gas oil, based on 100 parts by weight of bitumen or distillation residue obtained by distilling bitumen.

[0043] In one embodiment, the bitumen-derived transport pyrolysis mixture may, when using bitumen-derived distillation residue as a raw material, contain 0.1 to 5 parts by weight, 0.5 to 3 parts by weight, 1 to 2 parts by weight of hydrocarbon gas, 0.1 to 5 parts by weight, 0.5 to 3 parts by weight, 1 to 2 parts by weight of naphtha, 1 to 20 parts by weight, 3 to 15 parts by weight, 5 to 10 parts by weight of middle distillates, and 20 to 80 parts by weight, 30 to 70 parts by weight, 40 to 50 parts by weight of gas oil, based on 100 parts by weight of the distillation residue. The pyrolysis mixture having the above composition range may have excellent fluidity and may also be capable of producing more high value-added products from bitumen, but is not limited thereto.

[0044] In one embodiment, the bitumen-derived transport pyrolysis mixture may contain, when bitumen is used as a raw material, 0.05 to 5 parts by weight, 0.1 to 3 parts by weight, 0.2 to 2 parts by weight of hydrocarbon gas, 1 to 10 parts by weight, 2 to 8 parts by weight, 4 to 6 parts by weight of naphtha, 10 to 50 parts by weight, 15 to 40 parts by weight, 20 to 35 parts by weight of middle distillates, and 20 to 80 parts by weight, 30 to 70 parts by weight, 35 to 50 parts by weight of gas oil, per 100 parts by weight of bitumen.

[0045] In one embodiment, the pyrolysis mixture has a kinematic viscosity of 500,000 mm at 40°C. 2 / s may be less than that.

[0046] In one embodiment, when the pyrolysis mixture contains 5 to 20 wt% of moisture, the kinematic viscosity (at 40°C) of the pyrolysis mixture is 100 to 100,000 mm 2 / s, 1,000 to 80,000 mm 2 / s, 5,000 to 60,000 mm 2 / s, 10,000 to 55,000 mm 2 / s, but is not limited thereto. The pyrolysis mixture within the above-mentioned viscosity range may facilitate pipeline transport. The flow of the pyrolysis mixture within the pipeline becomes smoother, and it can be transported with less energy, which can significantly reduce pumping costs. In addition, it is preferred because it can transport a larger amount within the same amount of time, and the pressure and stress applied to pipeline equipment such as pumps and valves can be reduced, which can be advantageous in terms of equipment durability, but is not limited thereto.

[0047] In one embodiment, when the pyrolysis mixture does not contain moisture (0 wt%) or contains less than 5 wt% of moisture, the kinematic viscosity (at 40°C) of the pyrolysis mixture is 100,000 to 500,000 mm 2 / s, 150,000 to 400,000 mm 2 / s, 180,000 to 300,000 mm 2 / s, 200,000 to 250,000 mm 2 / s, and a pyrolysis mixture in the above viscosity range may be advantageous in terms of transport and is therefore preferred, but is not limited thereto.

[0048] In one embodiment, the pyrolysis mixture may have a kinematic viscosity reduction of 90% or more, 91% or more, 92% or more, or, although the upper limit is not particularly limited, 99.5% or less, 99% or less, or 98.5% or less compared to the distillation residue, and may be any value therebetween. For example, the kinematic viscosity may be 90 to 99.5%, 91 to 99%, or 92 to 98.5%, but is not limited thereto. Reducing the kinematic viscosity of the distillation residue within the above range is preferred because the fluidity of the distillation residue can be greatly improved, but is not limited thereto.

[0049] In one embodiment, the bitumen-derived pyrolysis mixture for transportation may have an API (American Petroleum Institute) gravity of 2 to 25, 3 to 20, or 4 to 10. A pyrolysis mixture having the API gravity range is preferred because it has a high energy density, thus increasing energy efficiency relative to transportation costs, and also has excellent transportation stability, but is not limited thereto.

[0050] In one embodiment, the pyrolysis mixture may have a C7 asphaltene content of 25 wt%, 24 wt% or less, 23 wt% or less, or a lower limit not particularly limited to, 15 wt% or more, 16 wt% or more, or 18 wt% or more, according to ASTM D3279, or any value therebetween. For example, the content may be 15 to 25 wt%, 16 to 24 wt%, or 18 to 23 wt%, but is not limited thereto. The pyrolysis mixture having the above C7 asphaltene content range may have a low viscosity and density, which facilitates transportation and refining processes, and may be preferred because it can reduce coke formation and have an excellent light oil yield, but is not limited thereto.

[0051] Another aspect of the present invention is a method for partially reforming bitumen, comprising a pyrolysis process step of injecting bitumen or bitumen-derived distillation residue and steam into a pyrolysis reactor and performing a pyrolysis reaction to obtain a pyrolysis mixture;

[0052] The above thermal decomposition process step is performed in a reactor having a bubble column, and a method for partially reforming bitumen is provided in which the steam is injected into the reactor through the bubble column.

[0053] The partially reformed pyrolysis mixture manufactured through the above bitumen partial reforming method may have a moisture content of 20 wt% or less and may be transported through a pipeline.

[0054] In addition, in one embodiment of the present invention, after the pyrolysis process step, a step of controlling the moisture content of the obtained pyrolysis mixture may be further included. At this time, methods for controlling the moisture content may include removing the moisture by performing processes such as distillation, three-phase separation, adsorption, membrane separation, evaporation, cooling condensation, and dehydrating agent treatment, but are not limited thereto. The pyrolysis mixture from which moisture has been removed may have a moisture content of less than 5 wt%, or substantially 0 wt%.

[0055] The reactor having the above-mentioned bubble column is, for example, a cylindrical reactor in which vapor is dispersed in the form of bubbles inside the reactor through a nozzle or a distribution plate at the bottom. The inside of the reactor maintains a nearly isothermal condition. In addition, the injected distillation residue oil and vapor may form a co-current flow that rises together from the bottom to the top of the reactor, but is not limited thereto.

[0056] In one embodiment, the pyrolysis process step may be to inject steam into the reactor through a bubble column in an amount of 1 to 100 parts by weight, 2 to 80 parts by weight, or 3 to 50 parts by weight, based on 100 parts by weight of bitumen or bitumen-derived distillation residue. When steam is injected in the above range to cause contact reaction with the distillation residue, heat transfer is uniformly distributed in the pyrolysis process step, so that the pyrolysis of the distillation residue is efficiently performed, and overheating or un-decomposed residues are prevented from remaining, resulting in incomplete pyrolysis. In addition, the viscosity of the distillation residue may be reduced more efficiently, but is not limited thereto.

[0057] In one embodiment, the pyrolysis process may be performed by injecting steam through a bubble column of a reactor at a superficial gas velocity of 0.05 to 10 cm / s, 0.1 to 5 cm / s, or 1 to 3 cm / s. Performing the pyrolysis process by injecting steam at the superficial gas velocity may allow for good mixing and sufficient contact between bitumen or bitumen-derived distillation residue oil and steam, thereby enabling efficient pyrolysis reaction, and may also allow for even heat transfer, thereby maintaining a uniform temperature distribution within the reactor. In addition, it may be possible to reduce the generation of coke by reducing C7 asphaltene, but is not limited thereto.

[0058] In one embodiment, the thermal decomposition process can be performed by injecting a mixed gas of steam and nitrogen through a bubble column of a reactor in the above-described gas velocity range.

[0059] In one embodiment, the thermal cracking process step may be performed under reactor pressure conditions of 5 to 80 barg, 8 to 50 barg, and 10 to 30 barg. When the thermal cracking process is performed under the above pressure condition range, the thermal cracking of bitumen or bitumen-derived distillation residue oil can proceed smoothly, thereby reducing coke formation, maximizing light oil yield, and lowering the viscosity of the thermal cracking mixture, and is therefore preferred, but is not limited thereto.

[0060] In one embodiment, the thermal decomposition process step may be performed under temperature conditions of 300 to 500°C, 350 to 450°C, or 400 to 450°C. When the thermal decomposition process is performed within the above temperature ranges, the thermal decomposition reaction rate may be optimized, and the viscosity of the thermal decomposition mixture may be reduced. In addition, coke formation may be prevented and the light oil yield may be increased, but is not limited thereto.

[0061] In one embodiment, the thermal decomposition process step may be performed with a residence time of 5 to 250 minutes, 10 to 200 minutes, or 30 to 100 minutes. When the thermal decomposition process is performed within the above residence time range, the yield of high value-added products such as hydrocarbon gas, naphtha, heavy oil, and gas oil converted from distillation residue oil may increase, and further, the formation of unnecessary byproducts such as coke or heavy residues due to excessive decomposition of raw materials may be prevented, so this is preferred, but is not limited thereto.

[0062] In one embodiment, the thermal cracking process step may be performed by further including one or more mixed catalysts selected from the group consisting of catalysts of aluminum silicate, zeolite, molybdenum (Mo), nickel (Ni), iron (Fe), vanadium (V), tungsten (W), manganese (Mn), copper (Cu), zinc (Zn), and cobalt (Co). For example, the catalyst may be a mixed catalyst such as Fe2O3 / NiO, Fe2O3 / Zeolite, Ni / Al2O3, Ni-Mo / Al2O3, Co3O4, etc., but is not limited thereto. When the thermal cracking process is performed including the catalyst, the distillate residue oil can rapidly proceed with the thermal cracking reaction rate by steam, and the conversion rate into a light oil component can be increased, so that it is preferred, but is not limited thereto.

[0063] In one embodiment, the catalyst may be injected into the reactor in an amount of 0.005 to 0.1 part by weight, 0.01 to 0.05 part by weight, or 0.02 to 0.05 part by weight, based on 100 parts by weight of bitumen or bitumen-derived distillate residue. Injecting the catalyst in the above content range is preferred because it can reduce the viscosity of the distillate residue and improve the yield of light oil, but is not limited thereto.

[0064] In one embodiment, the bitumen partial reforming method may further include one or more processes selected from the group consisting of a vacuum distillation unit (VDU), an atmospheric distillation unit (ADU), a hydrodesulfurization process (HDT), a desalting and dehydration process, a coking process, a refining process, and a solvent deasphalting (SDA) process, but is not limited thereto. In addition, the processes may be performed regardless of the order. Process diagrams relating to one embodiment of the bitumen partial reforming method according to the present invention are shown in FIGS. 1 to 4. The process diagrams of FIGS. 1 to 4 are merely examples for explaining the present invention in more detail and are not limiting thereto.

[0065] The combination of the above thermal cracking process and solvent deasphalting process is complementary, and by combining the two processes, effects such as increasing light oil yield, suppressing coke formation, and improving oil stability can be achieved.

[0066] The solvents used in the above solvent deasphalting process are mainly non-polar or slightly polar hydrocarbon solvents, such as propane, butane, pentane, hexane, heptane, isopentane, isohexane, dichloromethane, and carbon tetrachloride (CCl4), and there is no limitation on the solvent as long as it has a solubility suitable for separating high molecular weight substances such as asphaltenes.

[0067] In one embodiment, when a solvent deasphalting process is performed before a pyrolysis process, it may be possible to produce light oil products while preventing coke formation during the pyrolysis process. The pyrolysis process can improve the viscosity and API (American Petroleum Institute) gravity of bitumen through high-temperature pyrolysis, but coke may be formed during this process, which reduces process efficiency. Therefore, it may be possible to suppress coke formation by applying a solvent deasphalting process to remove asphaltenes. In addition, although the pyrolysis process can increase the yield of light hydrocarbons (light naphtha oil) through pyrolysis, its effect is limited due to the decomposition limit of asphaltenes. However, applying the pyrolysis process after removing asphaltenes in the solvent deasphalting process may further improve the yield of light oil.

[0068] In one embodiment, when the solvent deasphalting process is performed after the pyrolysis process, applying the residue after the pyrolysis process to the solvent deasphalting process may further reduce the viscosity and density of the partially modified bitumen and more effectively separate light oil and asphaltene.

[0069] The present invention will be described in more detail based on the following examples and comparative examples. However, the following examples and comparative examples are merely illustrative examples for further explaining the present invention, and the present invention is not limited by the following examples and comparative examples.

[0070] [measurement method]

[0071] 1. Kinematic viscosity measurement method

[0072] The kinematic viscosity of bitumen or bitumen-derived distillation residue and pyrolysis mixture was measured at a temperature of 40 ℃ using a Dynamic Stress Rheometer (Rheostress 6000; Thermo Fisher Scientific).

[0073] 2. API gravity measurement method

[0074] API gravity of bitumen or bitumen-derived distillation residue and pyrolysis mixture was measured using a density-specific gravity meter (DMA 4500 & DMA HP; Anton Paar) according to ASTM D5002-99.

[0075] 3. Moisture content measurement method

[0076] The moisture content of the pyrolysis mixture was measured using a moisture analyzer (Karl Fischer Titrator, Metrohm 852 Titrando - Metrohm 860 KF Thermoprep).

[0077] 4. Method for measuring components of pyrolysis mixture

[0078] Boiling point distribution analysis of the pyrolysis mixture was performed according to ASTM D7500 (7890A GC system, Agilent technologies).

[0079] [Example 1]

[0080] For 100 parts by weight of bitumen-derived vacuum residue, 18 parts by weight of steam was injected into a pyrolysis reactor equipped with a bubble column. The steam was injected at a gas linear velocity of 1.4 cm / s, and the pyrolysis process was performed at a reactor temperature of 400°C, a reaction pressure of 10 barg, and a residence time of 30 minutes (reactor volume = 1 L), thereby obtaining a pyrolysis mixture.

[0081] [Example 2]

[0082] A pyrolysis mixture was obtained by performing the same pyrolysis process as in Example 1 above, except that 0.02 parts by weight of Fe2O3 / NiO catalyst was additionally injected into the reactor for 100 parts by weight of bitumen-derived vacuum residue.

[0083] [Example 3]

[0084] A pyrolysis mixture was obtained by performing the same pyrolysis process as in Example 1 above, except that 3.5 parts by weight of steam was injected per 100 parts by weight of bitumen-derived depressurized residue.

[0085] [Example 4]

[0086] The pyrolysis mixture obtained in Example 1 was subjected to a rotary evaporator to remove all water vapor and moisture contained in the product, thereby producing a pyrolysis mixture having a moisture content of 0 wt%.

[0087] [Example 5]

[0088] The pyrolysis mixture obtained in Example 2 above was subjected to a rotary evaporator to remove all water vapor and moisture contained in the product, thereby producing a pyrolysis mixture having a moisture content of 0 wt%.

[0089] [Comparative Example 1]

[0090] A pyrolysis mixture was obtained by performing the same pyrolysis process as in Example 1 above, except that steam was not injected into the reactor.

[0091] Kinematic viscosity (mm) 2 / s) Kinematic viscosity reduction (%) C7 Asphaltene content (wt%) Moisture content (wt%) API vacuum residue 2,902,0580 (standard) 19.04 04 Example 151,946.8 98.21 19.75 155.58 Example 235,578.6 98.77 19.61 155.59 Example 3249,791.09 1.39 20.04 34.89 Example 4227,894.79 2.15 22.24 04.11 Example 5205,66 0.4 92.9 120.16 04.71 Comparative example 1290,911.6 89.98 22.8 105.56 Comparative example 2--21.2525-

[0092] In Table 1 above, the kinematic viscosity reduction amount of the examples was 90% or more, which is higher than that of the pyrolysis mixture (Comparative Example 1) after the existing pyrolysis process. In particular, the kinematic viscosity reduction amounts of Examples 1 and 2 were 98% or more, and it was confirmed that the fluidity was very excellent in the range of moisture content 5 to 20 wt%, and thus, it could provide a kinematic viscosity that is advantageous for pipeline transportation.

[0093] Examples 4 and 5 were performed to remove moisture for purification after the thermal decomposition process of Examples 1 and 2, respectively, and it was confirmed that the kinematic viscosity increased again and the API decreased.

[0094] In addition, it was confirmed that the asphaltene formation layer of the examples was suppressed compared to the comparative examples. Comparative Example 1 has a high API index, but a relatively high C7 asphaltene content, which increases the possibility of coke formation, and therefore, it can be expected to have lower actual process efficiency than the examples.

[0095] In the case of Comparative Example 2, which contained an excess amount of moisture compared to the example, the gas velocity was very high, so the product was not converted by the pyrolysis reactor and overflowed.

[0096] Table 2 below shows the components of the partially modified pyrolysis mixture (excluding moisture) through the non-point distribution analysis of Example 1.

[0097] Composition wt%GasHydrogen sulfide0.2Methane(C1)0.2Ethane(C2)0.2Propane(C3)0.4Isobutane(IC4)0.1C5+0.1Liquid(toluene soluble)Naphtha; IBP~117℃0.9Heavy oil; 177~343℃5.0Gas oil; 343~524℃29.6Vacuum residue; 524℃~63.3

[0098] In Table 2 above, it can be confirmed that the pyrolysis mixture of Example 1 was partially (36.7%) decomposed into naphtha, heavy oil, gas oil, and gas components.

[0099] As described above, the present invention has been described through specific matters and limited examples, but these are provided only to help a more general understanding of the present invention, and the present invention is not limited to the above examples, and those skilled in the art to which the present invention pertains can make various modifications and variations based on this description.

[0100] Therefore, the idea of ​​the present invention should not be limited to the described embodiments, and all things that are equivalent or equivalent to the following claims as well as the claims are considered to fall within the scope of the idea of ​​the present invention.

[0101] (Explanation of symbols)

[0102] (A) Distillation process

[0103] (B) Solvent deasphalting process

[0104] (C) Pyrolysis process

[0105] (D) Moisture control process

Claims

1. A thermal cracking mixture manufactured by mixing bitumen or bitumen-derived distillation residue and steam and thermally cracking it. The above pyrolysis mixture is a pyrolysis mixture containing moisture of 20 wt% or less.

2. In paragraph 1, The above pyrolysis mixture is a pyrolysis mixture containing 0 to 15 wt% of moisture.

3. In paragraph 1, The above pyrolysis mixture is a pyrolysis mixture in which more than 20% of the mass of bitumen or bitumen-derived distillation residue is converted into a mixture of hydrocarbon gas, naphtha, middle distillates, and gas oil.

4. In paragraph 1, The above bitumen-derived pyrolysis mixture for transportation is a pyrolysis mixture comprising 0.05 to 5 parts by weight of hydrocarbon gas, 0.1 to 10 parts by weight of naphtha, 1 to 50 parts by weight of middle distillates, and 20 to 80 parts by weight of gas oil, with respect to 100 parts by weight of bitumen or distillation residue obtained by distilling bitumen.

5. In paragraph 1, The above pyrolysis mixture has a kinematic viscosity of 500,000 mm at 40°C. 2 A pyrolysis mixture having a temperature of / s or less.

6. In paragraph 1, The above bitumen-derived pyrolysis mixture for transportation is a pyrolysis mixture having a kinematic viscosity reduction of 90% or more compared to distillation residue oil.

7. In paragraph 1, The above bitumen-derived pyrolysis mixture for transportation is a pyrolysis mixture having an API (American Petroleum Institute) gravity of 2 to 25.

8. In paragraph 1, The above pyrolysis mixture is a pyrolysis mixture containing a C7 asphaltene content of 25 wt% or less according to ASTM D3279.

9. A method for partially reforming bitumen, comprising a pyrolysis process step of injecting bitumen or bitumen-derived distillation residue and steam into a pyrolysis reactor and performing a pyrolysis reaction to obtain a pyrolysis mixture; A method for partially reforming bitumen, wherein the above thermal decomposition process step is performed in a reactor having a bubble column, and the steam is injected into the reactor through the bubble column.

10. In paragraph 9, The above thermal decomposition process step is a method for partially reforming bitumen, wherein steam is injected into a reactor through a bubble column in an amount of 1 to 100 parts by weight per 100 parts by weight of bitumen or bitumen-derived distillation residue oil.

11. In paragraph 9, A method for partially reforming bitumen, wherein the above thermal decomposition process step is performed under pressure conditions of 5 to 80 barg.

12. In paragraph 9, A method for partially reforming bitumen, wherein the above thermal decomposition process step is performed at a temperature of 300 to 500°C.

13. In paragraph 9, A method for partially reforming bitumen, wherein the above thermal decomposition process step is performed with a residence time of 5 to 250 minutes.

14. In paragraph 9, A method for partially reforming bitumen, wherein the above thermal decomposition process step is performed by further including one or more mixed catalysts selected from the group consisting of catalysts of the aluminum silicate, zeolite, molybdenum (Mo), nickel (Ni), iron (Fe), vanadium (V), tungsten (W), manganese (Mn), copper (Cu), zinc (Zn), and cobalt (Co) series.

15. In paragraph 9, A method for partially reforming bitumen, wherein the above mixed catalyst is included in an amount of 0.005 to 0.1 parts by weight per 100 parts by weight of bitumen or bitumen-derived distillation residue oil to perform a thermal decomposition process.

16. In paragraph 9, The bitumen partial reforming method further comprises a step of controlling the moisture content of the obtained pyrolysis mixture after the pyrolysis process step.

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