Process for heavy oil solid-liquid separation, system for heavy oil processing and method thereof

Abstract

The present application relates to the technical field of petroleum chemical industry, in particular to a hydrocyclone and application thereof, a heavy oil solid-liquid separation method, a heavy oil processing system and method thereof; the hydrocyclone comprises a shell, and a material feeding pipe, a solvent feeding pipe, a light liquid phase discharging pipe and a heavy liquid phase discharging pipe arranged on the shell; wherein the shell comprises a first straight cylinder segment arranged on the top and a conical segment arranged on the bottom. The hydrocyclone provided by the present application can effectively improve the desolidification rate of the material; meanwhile, the hydrocyclone is used for heavy oil solid-liquid separation, which not only effectively improves the desolidification rate of the heavy oil, but also improves the quality of the light liquid phase oil product.

Description

Technical Field

[0001] This invention relates to the field of petrochemical technology, specifically to a hydrocyclone separator and its application, a method for solid-liquid separation of heavy oil, and a system and method for heavy oil processing. Background Technology

[0002] As oil products become increasingly heavier, simple thermal processing methods can lead to severe coking, necessitating the addition of various catalysts to lower the reaction energy barrier and temperature. This results in the production of various high-viscosity heavy oil products containing solid catalyst particles, such as catalytic cracking slurry and liquid products from slurry bed reactors. These heavy oils are rich in aromatics and have low gum and asphaltenes content, making them highly valuable for economic use. They can be used as feedstocks in petrochemical production processes and as high-quality raw materials for asphalt modifiers, reinforcing agents, and activators. The liquid products from slurry bed reactors require separation of the solid catalyst, which is then pumped back into the reactor for recycling. However, the presence of solid catalyst particles can cause numerous problems such as coking, wear, and blockage in pipelines and furnaces. Therefore, separating these solid particles from high-viscosity heavy oils is an urgent problem to be solved.

[0003] Existing heavy oil desolidification technologies mainly include additive sedimentation, filtration separation, centrifugal separation, distillation separation, and electrostatic separation. Among these, filtration technology uses a filter medium to intercept catalyst particles in the oil slurry to achieve desolidification. This method features simple equipment, high separation efficiency, stable operation, and minimal impact of oil slurry properties on separation performance. However, it has high initial investment, and filter elements and cloths are easily clogged by colloids, asphaltenes, and fine catalysts in the oil slurry, leading to a gradual decrease in throughput. Replacing or backwashing the filter medium requires periodic shutdowns or switching, making it unsuitable for continuous operation. CN202010278509.8 discloses a special membrane filter technology that enables filtration of oil slurry without interruption of flow, but the equipment is complex and costly.

[0004] Electrostatic separation is poorly suited for oil slurries with high resin and asphalt content or high water content, resulting in unstable separation efficiency. Furthermore, it incurs high equipment investment and maintenance costs, making industrialization difficult at present. Distillation is simple to operate and has a mature process, but it has a low extraction rate, requires vacuum distillation equipment, incurs high equipment investment, and solid particles tend to deposit in the heating furnace and heat exchanger.

[0005] Additive sedimentation is an improvement on traditional natural sedimentation. Adding diluents to the slurry can significantly reduce the system viscosity and shorten sedimentation time. CN201910500375.7 discloses a method for removing solids from slurry, in which the slurry is mixed with highly soluble organic solvents such as toluene and catalytic diesel at 40-60℃ for sedimentation, followed by separation of solid waste residue using centrifugation. CN201010613973.4 discloses a method for removing catalyst powder from catalytic cracking slurry, using aromatic solvents such as benzene and xylene to dilute and settle the catalytic slurry, achieving a solids removal rate of over 98%. However, the strong dissolving power of aromatic solvents will dissolve all impurities such as gums and asphaltenes, requiring further separation and removal later. CN201510144811.3 discloses a pretreatment method for catalytic slurry, using C3-C5 light hydrocarbon fractions as solvents for subcritical extraction of the slurry to prepare a purified slurry that is essentially free of asphaltenes and solid particles. However, the sedimentation time is long and the yield is low. Although the sedimentation of additives can improve the desolidification efficiency, the sedimentation rate is still relatively slow, and centrifugation equipment is needed to accelerate it, which increases the investment in equipment.

[0006] Centrifugal separation methods are mainly divided into centrifugal sedimentation and hydrocyclone separation. CN97121100.0 discloses a method for separating oil slurry using a high-temperature centrifuge, achieving a solidification rate as high as 99%. However, the centrifuge has a small throughput and is difficult to maintain, making it unsuitable for large-scale industrial application. Hydrocyclone separation offers a large throughput and compact structure, but for high-viscosity heavy oil systems, the solidification rate is only 55-82%. CN200910092042.1 discloses a hydrocyclone separator for slurry bed reactors. Due to its low solidification efficiency, the liquid products after two-stage hydrocyclone separation require further membrane separation to meet the solidification requirements.

[0007] In summary, the difficulty in desolidification of high-viscosity heavy oil systems lies in the fact that existing technologies cannot simultaneously achieve high desolidification rates, high throughput, and continuous operation. Summary of the Invention

[0008] The purpose of this invention is to overcome the above-mentioned technical problems and provide a hydrocyclone separator and its application, a method for solid-liquid separation of heavy oil, and a system and method for heavy oil processing. The hydrocyclone separator not only effectively removes solid particles from materials and improves the solidification efficiency, but also has the characteristics of short solidification time, large processing capacity per unit time, and high yield of solidified materials.

[0009] To achieve the above objectives, a first aspect of the present invention provides a hydrocyclone separator, the hydrocyclone separator comprising: a shell, and a material inlet pipe, a solvent inlet pipe, a light liquid phase outlet pipe and a heavy liquid phase outlet pipe disposed on the shell; wherein the shell comprises a first straight cylindrical section disposed on the upper part and a conical section disposed on the lower part.

[0010] Preferably, one end of the light liquid phase discharge pipe extends into the housing and into the conical section, while the other end extends out of the top of the housing.

[0011] Preferably, the ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell is ≥0.5:1.

[0012] Preferably, the extended portion of the light liquid phase discharge pipe is provided with an opening.

[0013] Preferably, the housing further includes a second straight section disposed below the conical section.

[0014] Preferably, the material feed pipe and the solvent feed pipe are each independently and tangentially arranged in the upper part of the first straight section, and the material feed pipe and the solvent feed pipe are arranged opposite to each other.

[0015] Preferably, the hydrocyclone separator further includes a solvent backwash feed pipe disposed on the second straight section.

[0016] The second aspect of the present invention provides an application of the hydrocyclone separator provided in the first aspect in the solid-liquid separation of heavy oil.

[0017] A third aspect of the present invention provides a method for solid-liquid separation of heavy oil, wherein the method is carried out in a hydrocyclone separator provided in the first aspect, wherein the method includes: heavy oil entering through a material feed pipe and solvent entering through a solvent feed pipe contacting and mixing in a first straight section, the resulting mixture being hydrocycloned in a conical section, the resulting solvent-rich light liquid phase being discharged from a light liquid phase outlet pipe, and the resulting solid-rich heavy liquid phase being discharged from a heavy liquid phase outlet pipe.

[0018] Preferably, the weight ratio of the heavy oil to the solvent is 0.5-4:1.

[0019] The fourth aspect of the present invention provides a system for heavy oil processing, the system comprising: a hydrocyclone separator provided in the first aspect, a solvent separation tower and a first stripping tower sequentially connected to the top of the hydrocyclone separator, and a second stripping tower and an asphalt gasification furnace sequentially connected to the bottom of the hydrocyclone separator; The hydrocyclone separator is used to mix heavy oil and solvent and perform hydrocyclone separation to obtain a solvent-rich light liquid phase and a solid-rich heavy liquid phase. The solvent separation tower is used to separate the solvent-rich light liquid phase, and the resulting crude purified oil enters the first stripping tower for first stripping to obtain purified oil. The second stripping tower is used to perform a second stripping of the solid-rich heavy liquid phase, and the resulting solid residue is fed into the asphalt gasification furnace for oxidation reaction to obtain crude syngas.

[0020] The fifth aspect of the present invention provides a method for processing heavy oil, the method being performed in the system provided in the fourth aspect, the method comprising the following steps: (1) Mix heavy oil and solvent and perform hydrocyclone separation to obtain a solvent-rich light liquid phase and a solid-rich heavy liquid phase; (2) The solvent-rich light liquid phase is subjected to solvent separation, and the crude purified oil obtained is subjected to first stripping to obtain purified oil; (3) The solid-rich heavy liquid phase is subjected to a second stripping, and the resulting solid residue is subjected to an oxidation reaction to obtain crude syngas.

[0021] Compared with the prior art, the present invention has the following advantages: (1) The hydrocyclone separator provided by the present invention, by providing a solvent feed pipe on the shell, especially limiting the tangential arrangement of the material feed pipe and the solvent feed pipe, allows the material and solvent to mix and perform hydrocyclone separation, which greatly reduces the viscosity of the mixed system and increases the density difference between the solid and liquid phases, making the solid particles in the material more inclined to accumulate at the bottom of the shell in the internal vortex, which can effectively improve the desolidification rate of the material; in particular, by optimizing the structural setting of the hydrocyclone separator, for example, limiting the length of the extension part of the light liquid phase discharge pipe, providing an opening in the extension part and a filter in the extension part, and limiting the second straight section of the shell, the hydrocyclone separator provided by the present invention integrates hydrocyclone separation, filtration, centrifugation and auxiliary agent sedimentation, which can more effectively improve the desolidification efficiency and is applicable to large-scale industrial production; (2) Using the hydrocyclone separator provided by the present invention for heavy oil solid-liquid separation not only effectively improves the desolidification rate of heavy oil, but also shortens the desolidification time, increases the throughput per unit time, and improves the quality of light liquid phase oil (i.e., purified oil). (3) The heavy oil processing system provided by the present invention fully processes the heavy oil so that after solid-liquid separation, the solvent-rich light liquid phase obtained is converted into high-purity purified oil; at the same time, the solid-rich heavy liquid phase obtained from solid-liquid separation is converted into crude syngas, thereby achieving high processing efficiency of heavy oil. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the structure of a hydrocyclone separator provided by the present invention; Figure 2 This is a schematic diagram of a heavy oil processing system provided by the present invention.

[0023] Explanation of reference numerals in the attached figures Detailed Implementation

[0024] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0025] In this invention, unless otherwise specified, the terms "first" and "second" do not indicate a sequence or limit the specific materials or steps; they are merely used to distinguish or indicate that these are not the same material or step. For example, "first" and "second" in "first straight section" and "second straight section" are used only to indicate that these are not the same straight section; similarly, "first" and "second" in "first stripping" and "second stripping" are used only to indicate that these are not the same stripping process.

[0026] In this invention, unless otherwise specified, the top of the container refers to 0-10% of the container from top to bottom; the upper part of the container refers to 10-40% of the container from top to bottom; the middle part of the container refers to 40-60% of the container from top to bottom; the lower part of the container refers to 60-90% of the container from top to bottom; and the bottom of the container refers to 90-100% of the container from top to bottom.

[0027] The first aspect of the present invention provides a schematic diagram of the structure of a hydrocyclone separator, as shown below. Figure 1 As stated, by Figure 1 It is known that the hydrocyclone separator includes: a shell A, and a material feed pipe B, a solvent feed pipe C, a light liquid phase discharge pipe D, and a heavy liquid phase discharge pipe F disposed on the shell A; wherein, the shell A includes: a first straight cylindrical section A-1 disposed on the upper part and a conical section A-2 disposed on the lower part.

[0028] The inventors of this invention have discovered that by setting a solvent feed pipe on the shell of the hydrocyclone separator, and especially by optimizing the position of the solvent feed pipe, the material and solvent are mixed and hydrocyclone separated, which significantly reduces the viscosity of the mixed system and increases the density difference between the solid and liquid phases. This causes the solid particles in the material to tend to accumulate towards the bottom of the shell in the internal vortex, which can effectively improve the desolidification rate of the hydrocyclone separation.

[0029] In this invention, unless otherwise specified, the material entering from the material inlet pipe and the solvent entering from the solvent inlet pipe exist in the shell (i.e., the first cylindrical section) in the form of a vortex, rotating and moving towards the conical section in a spiral pattern. As the material flows from the first cylindrical section into the conical section, the liquid rotation speed gradually increases due to the gradually decreasing inner diameter. When the liquid exhibits vortex motion, the radial pressure is unequal, with the highest pressure at the shell sidewall. Because the diameter of the heavy liquid phase outlet pipe at the bottom of the shell is small, not all the liquid can be discharged from it. Simultaneously, because a light liquid phase outlet pipe is provided at the top of the shell, a portion of the separated, less dense light liquid phase accumulates at the bottom of the shell and flows towards the lower pressure center, forming a spiral-shaped light liquid column that rotates and moves towards the light liquid phase outlet pipe, thus forming an internal vortex flow, and finally being discharged from the liquid phase outlet pipe. At the same time, the denser solids and heavy liquid phases move towards the shell sidewall due to centrifugal force, separating from the less dense liquid, and finally being discharged from the heavy liquid phase outlet pipe. This enables the separation of solids and liquids.

[0030] In this invention, to ensure solid-liquid mass transfer and purification effects, it is necessary to ensure that most of the internal swirling flow is completed within the light liquid phase discharge pipe. Preferably, as follows: Figure 1 As shown, the light liquid phase discharge pipe D is disposed at the top of the shell A, and one end of the light liquid phase discharge pipe D extends into the shell A and extends to the conical section A-2; more preferably, the ratio of the length of the extended portion of the light liquid phase discharge pipe D to the height of the shell A is ≥0.5:1, preferably 0.6-0.75:1. When the ratio is less than 0.5:1, the light liquid phase discharge pipe cannot receive internal swirling flow; when the height ratio is greater than 0.75:1, the light liquid phase discharge pipe easily receives solid particles and asphalt.

[0031] In this invention, unless otherwise specified, the extended portion of the light liquid phase discharge pipe refers to the portion of the light liquid phase discharge pipe located within the housing; the extended portion of the light liquid phase discharge pipe refers to the portion of the liquid phase discharge pipe outside the housing, that is, the portion not located within the housing.

[0032] In this invention, preferably, as follows: Figure 1 As shown, the extended portion of the light liquid phase discharge pipe D is provided with an opening. This design allows a small amount of solid particles and heavy liquid phase such as asphaltene carried up by the rising internal vortex to be ejected through the opening during internal vortex flow, while the less dense light liquid phase can also enter the internal vortex flow through the opening. Mass transfer between the internal and external vortices purifies the light liquid phase, which is then discharged from the other end of the light liquid phase discharge pipe.

[0033] In some embodiments of the present invention, preferably, the particle size of the pores is 5-10 mm and the porosity is 4-15%. This configuration can prevent the pores from being blocked by asphalt and / or solid particles.

[0034] In this invention, preferably, as follows: Figure 1 As shown, the other end of the light liquid phase discharge pipe D extends out of the top of the shell A, and a filter E is installed on the extended part of the pipe, which can effectively prevent the rising internal swirling flow from entraining solid particles and improve the quality of the light liquid phase oil flowing out from the top of the hydrocyclone separator.

[0035] In this invention, preferably, as follows: Figure 1 As shown, a light liquid phase discharge valve H is also installed on the extended portion of the light liquid phase discharge pipe D. In this invention, the light liquid phase discharge valve is used to automatically control and stabilize the pressure of the hydrocyclone separator; during the hydrocyclone separation process, the light liquid phase carries relatively less solid powder, reducing the difficulty of filtration and significantly reducing the number of times the filter needs to be cleaned or backwashed.

[0036] In some specific embodiments of the present invention, preferably, the extended portion of the light liquid phase discharge pipe is selected from two branches, and each branch is sequentially provided with the filter and the light liquid phase discharge valve. This arrangement facilitates line switching to replace the filter medium in the filter.

[0037] In this invention, preferably, as follows: Figure 1 As shown, the shell A further includes a second straight cylindrical section A-3 disposed below the conical section A-2, which is used to separate the heavy liquid phase components in the material by sedimentation, thereby improving the yield of the light component materials.

[0038] In some embodiments of the present invention, preferably, the height ratio of the first straight section to the conical section is 1:3-5. This setting ensures sufficient hydrocyclone separation after the heavy oil and solvent are mixed; a ratio that is too low would reduce the internal swirling intensity of the light liquid phase. In some embodiments of the present invention, more preferably, the height ratio of the first straight section, the conical section, and the second straight section is 0.15-0.2:0.6-0.7:0.25-0.1. This configuration results in a longer settling section, allowing the heavy liquid phase components to settle sufficiently; a shorter section would reduce the yield of the light component materials.

[0039] In some embodiments of the present invention, preferably, the inner diameter of the first straight section is 300-3000 mm, and the inner diameter of the second straight section is 40-600 mm.

[0040] In some embodiments of the present invention, preferably, the inner diameter ratio of the light liquid phase discharge pipe and the second straight cylindrical section is 1-4:1, for example, 1:1, 1.2:1, 1.5:1, 2:1, 2.5:1, 4:1, and any value within the range of any two values, preferably 1.2-2.5:1. In the present invention, when the inner diameter ratio is higher than 4:1, the flow rate of the heavy liquid phase will be too fast, reducing the sedimentation effect of the heavy liquid phase; when the inner diameter ratio is lower than 1:1, the internal swirling flow of the light liquid phase cannot be fully received.

[0041] In some embodiments of the present invention, preferably, the inner diameter ratio of the heavy liquid phase discharge pipe and the second straight section is 0.6-1.3:1, for example, 0.6:1, 0.8:1, 1:1, 1.1:1, 1.3:1, and any value within any range of any two values, preferably 0.8-1.1:1. In the present invention, the above-mentioned inner diameter ratio is relatively close; too high or too low a ratio will increase the pressure drop across the heavy liquid phase discharge pipe, causing local turbulence and affecting the separation effect.

[0042] In this invention, preferably, as follows: Figure 1 As shown, the material feed pipe B and solvent feed pipe C are each independently and tangentially arranged at the upper part of the first straight cylindrical section A-1, and are arranged opposite to each other. This arrangement increases the linear velocity of the internal vortex, thereby increasing the centrifugal force and simultaneously increasing the contact area between the material and the solvent, thus promoting the dissolution and dispersion of the material in the solvent.

[0043] In this invention, unless otherwise specified, tangential arrangement means that the material feed pipe and the solvent feed pipe are each independently perpendicular to the circumferential normal of the cross-section of the shell; radial arrangement means that the solvent backwash feed pipe is perpendicular to the central axis of the shell.

[0044] In this invention, preferably, as follows: Figure 1 As shown, the heavy liquid phase discharge pipe F is located below the shell A; more preferably, the heavy liquid phase discharge pipe F is located below the second straight section A-3; more preferably, the heavy liquid phase discharge pipe F is also provided with a heavy liquid phase discharge valve I for automatically controlling the discharge of heavy liquid phase components.

[0045] In some embodiments of the present invention, preferably, the first straight cylindrical section and the second straight cylindrical section are each independently selected from cylinders, and the conical section is selected from an inverted cone.

[0046] In this invention, preferably, as follows: Figure 1As shown, the hydrocyclone separator also includes a solvent backwash feed pipe G installed on the second straight section A-3. Because the hydrocyclone separator has a high linear velocity and a short contact time, the bottom heavy liquid phase often contains a large amount of lighter components; therefore, introducing fresh solvent to perform a secondary extraction of the heavy liquid phase in the second straight section can improve the purified oil yield.

[0047] In this invention, more preferably, such as Figure 1 As shown, the solvent backwash feed pipe G is radially positioned in the second straight section A-3. This arrangement results in a lower linear velocity, avoiding turbulence and thus preventing any impact on the quality of the purified oil.

[0048] In this invention, preferably, as follows: Figure 1 As shown, the hydrocyclone separator further includes a heating element J, wherein the heating element J is arranged in a ring outside the housing A and is located on the upper part of the housing A; more preferably, the heating element J is located below the material feed pipe B and the solvent feed pipe D.

[0049] In this invention, the heating component includes, but is not limited to, heating jackets, heating tiles, etc. The heating component increases the solubility of the solvent at the top of the hydrocyclone separator, causing non-ideal asphaltene, heavy gum, and other components to separate and be thrown onto the sidewalls with the internal swirling flow, eventually settling to the bottom of the hydrocyclone separator.

[0050] The second aspect of the present invention provides an application of the hydrocyclone separator provided in the first aspect in the solid-liquid separation of heavy oil.

[0051] A third aspect of the present invention provides a method for solid-liquid separation of heavy oil, wherein the method is carried out in a hydrocyclone separator provided in the first aspect, wherein the method includes: heavy oil entering through a material feed pipe and solvent entering through a solvent feed pipe contacting and mixing in a first straight section, the resulting mixture being hydrocycloned in a conical section, the resulting solvent-rich light liquid phase being discharged from a light liquid phase outlet pipe, and the resulting solid-rich heavy liquid phase being discharged from a heavy liquid phase outlet pipe.

[0052] In some embodiments of the present invention, preferably, the weight ratio of heavy oil to solvent is 0.5-4:1, for example, 0.5:1, 0.8:1, 1:1, 1.5:1, 2:1, 3:1, 4:1, and any value within any range of two such values, preferably 0.8-3:1, more preferably 1-2:1. Using these preferred conditions is more conducive to improving the desolventization rate of heavy oil, improving the quality of the solvent-rich light liquid phase, thereby improving the yield and quality of the purified oil.

[0053] In this invention, unless otherwise specified, the heavy oil is a high-viscosity heavy oil containing solids. Preferably, the heavy oil satisfies the following condition: (80°C) kinematic viscosity ≥ 50 mmHg. 2 / s, preferably 80-300mm 2 / s; solid content ≥500μg / g, preferably 1000-6000μg / g; asphaltene content ≥4wt%, preferably 4-10wt%; wherein, solid content includes, but is not limited to, solid powder, catalyst particles, etc.

[0054] In this invention, unless otherwise specified, the kinematic viscosity parameter is measured according to GB / T 11137; the solid content parameter is measured according to QSH 0741-2018; and the asphaltene content parameter is measured according to SHT 0266-1992.

[0055] In this invention, a wide range of heavy oil types can be selected, as long as the heavy oil meets the above-mentioned limitations. Preferably, the heavy oil is selected from at least one of catalytic slurry oil, slurry-bed hydrogenation liquid products, coal tar, and shale oil.

[0056] In this invention, the solvent is intended to extract the light components from the heavy oil in a liquid phase. Preferably, the solvent is selected from C5-C8 alkanes, more preferably from at least one of n-pentane, isopentane, cyclopentane, n-hexane, isohexane, cyclohexane, n-heptane, isoheptane, n-octane, and isooctane, more preferably n-pentane and / or n-hexane, and most preferably n-pentane and n-hexane.

[0057] In some embodiments of the present invention, preferably, the conditions for hydrocyclone separation include: a top temperature of 100-200°C, more preferably 120-150°C; a bottom temperature of 80-180°C, more preferably 110-140°C; and a pressure of 2-6 MPa, more preferably 3.5-5 MPa. All pressures refer to gauge pressure.

[0058] In some embodiments of the present invention, preferably, the ratio of the sum of the mass flow rates of the heavy oil and the solvent to the mass flow rate of the solid-rich heavy liquid phase is 1:0.75-0.95, for example, 1:0.75, 1:0.85, 1:0.88, 1:0.9, 1:0.95, and any value within the range of any two values, preferably 1:0.85-0.9. Using these preferred conditions is more conducive to improving the solidification efficiency of the heavy oil.

[0059] In some embodiments of the present invention, preferably, the linear velocity of the heavy oil is less than or equal to the linear velocity of the solvent; more preferably, the linear velocity of the heavy oil is 2-6 m / s, and the linear velocity of the solvent is 5-8 m / s. If the linear velocity of the mixture of heavy oil and solvent is too high, the contact time between the heavy oil and solvent will be too short, resulting in insufficient mixing and dispersion; if the linear velocity of the mixture of heavy oil and solvent is too low, the internal vortex intensity will be reduced, affecting the centrifugal separation effect. In the present invention, the linear velocity of the mixture of heavy oil and solvent is the sum of the linear velocities of the heavy oil and the solvent.

[0060] In some embodiments of the present invention, preferably, the method further includes: heating the heavy oil and the solvent independently before mixing; more preferably, the temperature of the heated heavy oil and the heated solvent is independently 100-180°C.

[0061] In some embodiments of the present invention, preferably, the method further includes: filtering the solvent-rich light liquid phase; more preferably, centrifuging the solvent-rich light liquid phase before filtration. This arrangement further removes the residual heavy liquid phase from the solvent-rich light liquid phase, thereby improving the quality of the purified oil.

[0062] In some embodiments of the present invention, preferably, the method further includes: settling the solid-rich heavy liquid phase to further separate the light liquid phase remaining in the solid-rich heavy liquid phase, thereby improving the yield of purified oil.

[0063] In some embodiments of the present invention, preferably, the method further includes: backwashing the rich solids heavy liquid phase and fresh solvent to remove the residual light liquid phase in the rich solids heavy liquid phase, thereby improving the yield of purified oil.

[0064] A third aspect of the present invention provides a schematic diagram of the structure of a heavy oil processing system, as shown below. Figure 2 As shown, the system includes: a hydrocyclone 5 provided in the first aspect, a solvent separation tower 6 and a first stripping tower 7 connected in sequence to the top of the hydrocyclone 5, and a second stripping tower 9 and an asphalt gasification furnace 10 connected in sequence to the bottom of the hydrocyclone 5. The hydrocyclone separator 5 is used to mix heavy oil I and solvent II and perform hydrocyclone separation to obtain solvent-rich light liquid phase III and solid-rich heavy liquid phase IV. The solvent separation tower 6 is used to separate the solvent-rich light liquid phase III, and the resulting crude purified oil VI enters the first stripping tower 7 for first stripping to obtain purified oil VII. The second stripping tower 9 is used to perform a second stripping of the solid-rich heavy liquid phase IV, and the resulting solid residue IX is fed into the asphalt gasification furnace 10 for oxidation reaction to obtain crude syngas XII.

[0065] According to the present invention, preferably, such as Figure 2 As shown, the system further includes: a heavy oil storage tank 1 connected to the material feed pipe of the hydrocyclone 5, and a solvent storage tank 2 connected to the solvent feed pipe of the hydrocyclone 5. The heavy oil storage tank 1 is used to store heavy oil I, and the solvent storage tank 2 is used to store solvent II.

[0066] According to the present invention, preferably, such as Figure 2As shown, the solvent storage tank 2 is also connected to the solvent backwash feed pipe of the hydrocyclone 5, which is used to backwash the solid-rich heavy liquid phase and the fresh solvent.

[0067] According to the present invention, preferably, such as Figure 2 As shown, the top of the solvent separation tower 6, the top of the first stripping tower 7, and the top of the second stripping tower 9 are each independently connected to the solvent storage tank 2, and are used to return the high-temperature solvent V obtained from the solvent separation, the first stripping solvent VIII obtained from the first stripping, and the second stripping solvent X obtained from the second stripping to the solvent storage tank 2, respectively.

[0068] According to the present invention, preferably, such as Figure 2 As shown, the system further includes: an oil pump 3 installed on the connecting pipe between the heavy oil storage tank 1 and the hydrocyclone 5, and a solvent pump 4 installed on the connecting pipe between the solvent storage tank 2 and the hydrocyclone 5. In this invention, the oil pump is used to first pressurize the heavy oil to obtain pressurized heavy oil; the solvent pump is used to second pressurize the solvent to obtain pressurized solvent. The pressures of the pressurized heavy oil and the pressurized solvent are each independently equal to the hydrocyclone separation pressure in the hydrocyclone (i.e., 2-6 MPa, preferably 3.5-5 MPa).

[0069] According to the present invention, preferably, such as Figure 2 As shown, the system further includes a catalytic hydrogenation unit 8 connected to the first stripping tower 7, used to refine the purified oil VII to obtain refined oil product XI.

[0070] The fifth aspect of the present invention provides a method for processing heavy oil, the method being performed in the system provided in the fourth aspect, the method comprising the following steps: (1) Mix heavy oil and solvent and perform hydrocyclone separation to obtain a solvent-rich light liquid phase and a solid-rich heavy liquid phase; (2) The solvent-rich light liquid phase is subjected to solvent separation, and the crude purified oil obtained is subjected to first stripping to obtain purified oil; (3) The solid-rich heavy liquid phase is subjected to a second stripping, and the resulting solid residue is subjected to an oxidation reaction to obtain crude syngas; In this invention, the conditions for the separation of heavy oil, solvent and hydrocyclone are all as defined above, and will not be elaborated further.

[0071] In this invention, the solvent separation aims to remove solvent from the solvent-rich light liquid phase. Preferably, the conditions for solvent separation include: a temperature of 220-280°C and a pressure of 4-5 MPa.

[0072] In some embodiments of the present invention, preferably, the conditions for the first stripping include: a temperature of 220-260°C and a pressure of 0.55-0.65 MPa.

[0073] According to the present invention, preferably, the purified oil has a solid content of ≤350μg / g, more preferably ≤50μg / g, an asphaltene content of ≤3.5wt%, more preferably ≤2.5wt%, and a yield of ≥77%, more preferably ≥83%.

[0074] In some embodiments of the present invention, preferably, the conditions for the second stripping include: a temperature of 240-280°C and a pressure of 0.55-0.65 MPa.

[0075] In some embodiments of the present invention, preferably, the conditions for the oxidation reaction include: a reaction temperature of 1250-1450°C and a time of 0.1-5 h.

[0076] According to the present invention, preferably, the method further includes: independently returning and mixing the high-temperature solvent obtained from the solvent separation, the first stripping solvent obtained from the first stripping, and the second stripping solvent obtained from the second stripping into the solvent.

[0077] According to the present invention, preferably, the method further includes: refining the purified oil obtained in step (2) to obtain refined oil. In the present invention, the refining method has a wide range of options, including but not limited to hydrorefining, and the refined oil includes but not limited to hydrotreated catalytic oil.

[0078] According to a particularly preferred embodiment of the present invention, a hydrocyclone separator is provided, the hydrocyclone separator comprising: a shell, and a material inlet pipe, a solvent inlet pipe, a light liquid phase outlet pipe and a heavy liquid phase outlet pipe disposed on the shell; wherein, the shell comprises, from top to bottom, a first cylindrical section, a conical section and a second cylindrical section; One end of the light liquid phase discharge pipe extends into the housing and into the conical section, while the other end extends out of the top of the housing. The ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell is 0.6-0.75:1; the extended portion of the light liquid phase discharge pipe is provided with an opening. The height ratio of the first straight section, the conical section, and the second straight section is 0.15-0.2: 0.6-0.7: 0.25-0.1. A solvent backwashing feed pipe is radially arranged on the second straight section; The material feed pipe and the solvent feed pipe are each independently and tangentially arranged on the upper part of the housing, and the material feed pipe and the solvent feed pipe are arranged opposite to each other.

[0079] The present invention will be described in detail below through embodiments.

[0080] Example 1 Heavy oil processing system ,like Figure 1-2 As shown, the system includes: a heavy oil storage tank, an oil pump, a hydrocyclone separator, a solvent separation tower and a first stripping tower connected in sequence to the top of the hydrocyclone separator, and a second stripping tower and an asphalt gasification furnace connected in sequence to the bottom of the hydrocyclone separator. The solvent storage tank is also connected to the solvent backwash feed pipe of the hydrocyclone separator; the top of the solvent separation tower, the top of the first stripping tower, and the top of the second stripping tower are each independently connected to the solvent storage tank. The aforementioned hydrocyclone separator includes: a shell, which consists of a first cylindrical section, a conical section, and a second cylindrical section from top to bottom; a material feed pipe and a solvent feed pipe are positioned opposite each other and tangentially at the upper part of the first cylindrical section; one end of a light liquid phase discharge pipe extends into the shell and into the conical section, with an opening in the extended portion, and the other end extends out of the top of the shell, with a filter and a light liquid phase discharge valve sequentially installed on the extended portion; a heavy liquid phase discharge pipe is located below the second cylindrical section, and a heavy liquid phase discharge valve is also installed on the heavy liquid phase discharge pipe; a solvent backwash feed pipe is radially arranged in the second cylindrical section; and a heating element is annularly arranged around the outer side of the shell, located below the material feed pipe and the solvent feed pipe.

[0081] The ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell is 0.7:1; the particle size of the aforementioned openings is 8 mm, and the porosity is 10%. The height ratio of the first straight section, the conical section, and the second straight section is 0.15:0.7:0.15; the inner diameter of the first straight section is 1000 mm, and the inner diameter of the second straight section is 200 mm; the inner diameter ratio of the light liquid phase discharge pipe to the second straight section is 2:1; the inner diameter ratio of the heavy liquid phase discharge pipe to the second straight section is 1:1. The heavy oil processing method is carried out in the above system. The method includes the following steps: (1) Heated heavy oil (Shijiazhuang catalytic slurry, temperature 140℃, linear velocity 4m / s, composition listed in Table 1) and heated solvent (temperature 140℃, linear velocity 6m / s, n-pentane) were mixed at a weight ratio of 1.5:1 and subjected to hydrocyclone separation (top temperature 150℃, bottom temperature 140℃, pressure 4.5MPa). The resulting light liquid phase containing solids was centrifuged and filtered to obtain a solvent-rich light liquid phase. The resulting heavy liquid phase containing solids was subjected to sedimentation and backwashing to obtain a solid-rich heavy liquid phase. (2) The above-mentioned solvent-rich light liquid phase is subjected to solvent separation (temperature 240℃, pressure 4MPa), and the crude purified oil is subjected to first stripping (temperature 240℃, pressure 0.6MPa) to obtain purified oil S1; (3) The above-mentioned solid-rich heavy liquid phase is subjected to a second stripping (temperature 260℃, pressure 0.6MPa), and the resulting solid residue is subjected to an oxidation reaction (temperature 1350℃, time 2h) to obtain crude syngas P1. The ratio of the sum of the mass flow rates of the heavy oil and solvent to the mass flow rate of the solid-rich heavy liquid phase is 1:0.85. Among them, the high-temperature solvent obtained by solvent separation, the first stripping solvent obtained by the first stripping and the second stripping solvent obtained by the second stripping are all returned and mixed into the above solvents; The physical properties of purified oil S1 are listed in Table 2; the CO / H2 ratio in crude syngas P1 is 0.47 / 0.45.

[0082] Example 2 The system according to Example 1; The method of Example 1 was followed, except that the solvent was replaced with n-hexane, the weight ratio of heated heavy oil to heated solvent was replaced with 1:1, the hydrocyclone separation conditions were replaced with a top temperature of 120°C, a bottom temperature of 110°C, and a pressure of 4 MPa, and the mass flow ratio of the above-mentioned solid-rich heavy liquid phase and heavy oil was replaced with 0.9:1, with the other conditions remaining the same, to obtain purified oil S2 and crude syngas P2.

[0083] The physical properties of purified oil S2 are listed in Table 2; the CO / H2 ratio of crude syngas P2 is 0.48 / 0.42.

[0084] Example 3 The system according to Example 1; The method of Example 1 was followed, except that the ratio of the sum of the mass flow rates of the heavy oil and solvent to the mass flow rate of the solid-rich heavy liquid phase was 1:0.8, and the other conditions were the same, to obtain purified oil S3 and crude syngas P3.

[0085] The physical properties of purified oil S3 are listed in Table 2; the CO / H2 ratio in crude syngas P3 is 0.47 / 0.45.

[0086] Example 4 The system according to Example 1; Following the method of Example 1, except that the weight ratio of heated heavy oil to heated solvent was replaced with 0.8:1, while the other conditions remained the same, purified oil S4 and crude syngas P4 were obtained.

[0087] The physical properties of purified oil S4 are listed in Table 2; the CO / H2 ratio of crude syngas P4 is 0.48 / 0.42.

[0088] Example 5 The system according to Example 1; Following the method of Example 1, except that the weight ratio of heated heavy oil to heated solvent was replaced with 3.5:1, while the other conditions remained the same, purified oil S5 and crude syngas P5 were obtained.

[0089] The physical properties of purified oil S5 are listed in Table 2; the CO / H2 ratio of crude syngas P5 is 0.46 / 0.43.

[0090] Example 6 The system according to Example 1 is different except that the ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell is replaced with 0.5:1; Purified oil S6 and crude syngas P6 were obtained according to the method of Example 1.

[0091] The physical properties of purified oil S6 are listed in Table 2; the CO / H2 ratio of crude syngas P6 is 0.45 / 0.43.

[0092] Example 7 The system according to Embodiment 1 differs in that the light liquid phase discharge pipe does not have an opening along the length of its extension into the housing; The method of Example 1 is the same, except that in step (1), the solid-light liquid phase is filtered only, while the other conditions are the same, to obtain crude syngas P7.

[0093] The physical properties of purified oil S7 are listed in Table 2; the CO / H2 ratio of crude syngas P7 is 0.46 / 0.43.

[0094] Example 8 The system according to Example 1 differs in that the aforementioned housing does not include the second straight section and the solvent backwash feed pipe; The method of Example 1 is followed, except that the solid-containing heavy liquid phase in step (1) is used as the solid-rich heavy liquid phase, and the other conditions are the same, to obtain purified oil S8 and crude syngas P8.

[0095] The physical properties of purified oil S8 are listed in Table 2; the CO / H2 ratio of crude syngas P8 is 0.49 / 0.43.

[0096] Example 9 The system according to Embodiment 1 differs in that the height ratio of the first cylindrical section, the conical section, and the second cylindrical section is replaced with 0.4:0.5:0.1; Purified oil S9 and crude syngas P9 were obtained according to the method of Example 1.

[0097] The physical properties of purified oil S9 are listed in Table 2; the CO / H2 ratio of crude syngas P9 is 0.5 / 0.42.

[0098] Comparative Example 1 The system according to Example 1 differs in that the hydrocyclone separator is replaced with a conventional hydrocyclone separator, that is, it does not contain a solvent feed pipe, a second straight section and a solvent backwash feed pipe, and the light liquid phase discharge pipe is located at the top of the shell.

[0099] The heavy oil shown in Example 1 was subjected to hydrocyclone separation at a temperature of 150°C and a pressure of 1 MPa to obtain a light liquid phase and a solid-rich heavy liquid phase. The mass flow ratio of the solid-rich heavy liquid phase to the heavy oil was controlled to be 0.85:1. The light liquid phase is used as purified oil DS1; the solid-rich heavy liquid phase is oxidized to obtain crude syngas DP1. The physical properties of purified oil DS1 are listed in Table 2; the CO / H2 ratio of crude syngas DP1 is 0.49 / 0.41.

[0100] Comparative Example 2 The system is the same as in Example 2, except that the hydrocyclone is replaced with a conventional settling tower.

[0101] The heavy oil shown in Example 2 was processed in the above system. The method included: mixing the heavy oil and n-hexane at a weight ratio of 1:1, and then entering a settling tower for settling (temperature 120°C, pressure 4 MPa). The resulting solvent-rich light liquid phase and solid-rich heavy liquid phase flowed out from the top and bottom of the settling tower, respectively, wherein the mass flow ratio of the solid-rich heavy liquid phase to the heavy oil was 0.9:1. The above-mentioned solvent-rich light liquid phase was subjected to step (2) of Example 1 to obtain purified oil DS2; The above-mentioned solid-rich heavy liquid phase was processed according to step (3) of Example 1 to obtain crude syngas DP2; The physical properties of purified oil DS2 are listed in Table 2; the CO / H2 ratio of crude syngas DP2 is 0.49 / 0.42.

[0102] Table 1

[0103] Table 2

[0104] Continued from Table 2

[0105] As shown in Table 2, comparing Comparative Example 1 and Example 1, under the same conditions of raw materials, temperature, and yield, the purified oil slurry obtained in Comparative Example 1 has a significantly higher solid content and asphaltene content than that in Example 1. This indicates that introducing additives into a conventional hydrocyclone can significantly reduce the viscosity and solid-liquid density difference of the system, thereby improving the efficiency of centrifugal desolvation and achieving a high desolvation rate. Furthermore, because this invention adds a series of methods to the conventional hydrocyclone separator, such as top heating, internal and external cyclone mass transfer purification, and bottom settling backwashing, the yield and quality of the purified oil are further improved.

[0106] Comparing Comparative Example 2 and Example 2, under identical conditions of raw materials, temperature, and pressure, the purified oil slurry obtained in Comparative Example 2 had a higher solids content and a higher asphaltene content than that in Example 2, but the settling time was as long as 6 hours. This indicates that compared to additive settling, the heavy oil desolidification device provided by this invention, due to the use of hydrocyclone separation, greatly improves the solid-liquid separation speed, shortens the desolidification time, and increases the throughput.

[0107] Compared to Example 1, Example 3, by adjusting the ratio of the sum of the mass flow rates of heavy oil and solvent to the mass flow rate of the solid-rich heavy liquid phase within a non-preferred protection range, produced purified oil S3 with little change in quality, but a significant decrease in yield.

[0108] Compared to Example 1, Example 4, by adjusting the weight ratio of heavy oil to solvent within a non-optimal protection range, showed little change in the yield of the purified oil S4, but a significant change in quality. This was mainly due to the reduced weight ratio of heavy oil to solvent, which resulted in insufficient dissolving power of the heavy oil, failing to effectively separate the gums and asphaltenes in the heavy oil, leading to increased viscosity of the light oil phase and consequently, an increase in solid content.

[0109] Compared to Example 1, Example 5, by adjusting the weight ratio of heavy oil and solvent within a non-preferred protection range, produced purified oil S5 with little change in quality, but the yield was slightly reduced.

[0110] Compared to Example 1, Example 6, by adjusting the ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell within a non-preferred protection range, resulted in little change in the yield of the purified oil S6, but the quality was poor. This was mainly because the extended portion of the light liquid phase discharge pipe was too short to fully receive the internal swirling flow of the light liquid phase, leading to poor quality of the purified oil.

[0111] Compared to Example 1, Example 7 does not have an opening in the extension part of the light liquid phase discharge pipe, resulting in poorer quality of the purified oil S7. This is mainly because the solid-containing light liquid phase cannot be centrifuged and discharged, leading to an increase in the solid content and asphaltene content in the purified oil S7.

[0112] Compared to Example 1, Example 8 sets up a hydrocyclone separator that does not include a second straight section and a solvent backwash feed pipe, resulting in a lower quality purified oil S8, mainly reflected in the increased solid content and asphaltene content in purified oil S8.

[0113] Compared to Example 1, Example 9 adjusts the height ratio of the first straight section, the conical section, and the second straight section, resulting in a lower quality purified oil S9. This is mainly because the conical section is too short, which prevents sufficient swirling and settling, and easily causes backmixing, leading to an increase in the solid content and asphaltene content in the purified oil S9.

[0114] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for solid-liquid separation of heavy oil, characterized in that, The method is carried out in a hydrocyclone separator, wherein the method includes: heavy oil entering through the material feed pipe and solvent entering through the solvent feed pipe contacting and mixing in the first straight section; the resulting mixture undergoing hydrocyclone separation in the conical section; the resulting solvent-rich light liquid phase being discharged from the light liquid phase outlet pipe; and the resulting solid-rich heavy liquid phase being discharged from the heavy liquid phase outlet pipe; and the solid-rich heavy liquid phase and fresh solvent being backwashed. The hydrocyclone separator includes: a shell, and a material inlet pipe, a solvent inlet pipe, a light liquid phase outlet pipe and a heavy liquid phase outlet pipe disposed on the shell; The housing includes: a first straight cylindrical section disposed on the top and a conical section disposed on the bottom; One end of the light liquid phase discharge pipe extends into the housing and into the conical section, while the other end extends out of the top of the housing. The ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell is 0.6-0.75:1; The light liquid phase discharge pipe has an opening in the extension part; The housing further includes a second straight cylindrical section disposed below the conical section, wherein the inner diameter ratio of the light liquid phase discharge pipe to the second straight cylindrical section is 1.2-2.5:1; The hydrocyclone separator further includes a solvent backwash feed pipe disposed on the second straight section.

2. The method according to claim 1, wherein, The aperture of the opening is 5-10 mm, and the porosity is 4-15%. And / or, a filter is provided on the pipeline of the extended portion of the light liquid phase discharge pipe; And / or, a light liquid phase discharge valve is also provided on the pipeline of the extended portion of the light liquid phase discharge pipe.

3. The method according to claim 1, wherein, The height ratio of the first straight section to the conical section is 1:3-5; And / or, the height ratio of the first straight section, the conical section, and the second straight section is 0.15-0.2: 0.6-0.7: 0.25-0.

1.

4. The method according to claim 3, wherein, The inner diameter of the first straight section is 300-3000mm, and the inner diameter of the second straight section is 40-600mm; And / or, the inner diameter ratio of the heavy liquid phase discharge pipe and the second straight section is 0.6-1.3:

1.

5. The method according to claim 4, wherein, The ratio of the inner diameter of the heavy liquid phase discharge pipe to the inner diameter of the second straight section is 0.8-1.1:

1.

6. The method according to claim 3, wherein, The material feed pipe and the solvent feed pipe are each independently and tangentially arranged in the upper part of the first straight section, and the material feed pipe and the solvent feed pipe are arranged opposite to each other; And / or, the heavy liquid phase discharge pipe is disposed below the housing; And / or, the heavy liquid phase discharge pipe is also equipped with a heavy liquid phase discharge valve.

7. The method according to claim 6, wherein, The heavy liquid phase discharge pipe is located below the second straight section.

8. The method according to any one of claims 3-7, wherein, The hydrocyclone separator further includes a heating component, wherein the heating component is arranged in a ring around the outer side of the housing and is located on the upper part of the housing; And / or, the heating element is located below the material feed pipe and the solvent feed pipe.

9. The method according to claim 8, wherein, The hydrocyclone separator further includes: the solvent backwash feed pipe is radially arranged in the second straight section.

10. The method according to claim 1, wherein, The weight ratio of the heavy oil to the solvent is 0.5-4:1; And / or, the heavy oil satisfies the following condition: kinematic viscosity at 80°C ≥ 50 mmHg. 2 / s; Solid content ≥500μg / g; Asphaltene content ≥4wt% And / or, the solvent is selected from C5-C8 alkanes.

11. The method according to claim 10, wherein, The weight ratio of the heavy oil to the solvent is 0.8-3:1; And / or, the heavy oil satisfies the following condition: kinematic viscosity at 80°C is 80-300 mmHg. 2 / s; solid content is 1000-6000 μg / g; asphaltene content is 4-10 wt% And / or, the solvent is selected from at least one of n-pentane, isopentane, cyclopentane, n-hexane, isohexane, cyclohexane, n-heptane, isoheptane, n-octane, and isooctane.

12. The method according to claim 11, wherein, The weight ratio of the heavy oil to the solvent is 1-2:1; And / or, the solvent is n-pentane and / or n-hexane.

13. The method according to claim 1, wherein, The conditions for the hydrocyclone separation include: top temperature of 100-200℃; bottom temperature of 80-180℃; and pressure of 2-6MPa. And / or, the ratio of the sum of the mass flow rates of the heavy oil and the solvent to the mass flow rate of the solid-rich heavy liquid phase is 1:0.75-0.95; And / or, the linear velocity of the heavy oil is less than or equal to the linear velocity of the solvent; And / or, the linear velocity of the heavy oil is 2-6 m / s, and the linear velocity of the solvent is 5-8 m / s.

14. The method according to claim 13, wherein, The conditions for the hydrocyclone separation include: a top temperature of 120-150℃; a bottom temperature of 110-140℃; and a pressure of 3.5-5 MPa. And / or, the ratio of the sum of the mass flow rates of the heavy oil and the solvent to the mass flow rate of the solid-rich heavy liquid phase is 1:0.85-0.

9.

15. The method according to claim 1, wherein, The method further includes heating the heavy oil and solvent independently before mixing.

16. The method according to claim 15, wherein, The temperatures of the heavy oil and the solvent after heating are each 100-180℃ independently.

17. The method according to claim 1, wherein, The method further includes filtering the solvent-rich light liquid phase.

18. The method according to claim 17, wherein, Prior to filtration, the solvent-rich light liquid phase is centrifuged.

19. The method according to claim 1, wherein, The method further includes: settling the solid-rich heavy liquid phase.

20. A system for processing heavy oil, characterized in that, The system includes: a hydrocyclone separator, a solvent separation tower and a first stripping tower connected in sequence to the top of the hydrocyclone separator, and a second stripping tower and an asphalt gasification furnace connected in sequence to the bottom of the hydrocyclone separator; The hydrocyclone separator includes: a shell, and a material inlet pipe, a solvent inlet pipe, a light liquid phase outlet pipe and a heavy liquid phase outlet pipe disposed on the shell; The housing includes: a first straight cylindrical section disposed on the top and a conical section disposed on the bottom; One end of the light liquid phase discharge pipe extends into the housing and into the conical section, while the other end extends out of the top of the housing. The ratio of the length of the extended portion of the light liquid phase discharge pipe to the height of the shell is 0.6-0.75:1; The light liquid phase discharge pipe has an opening in the extension part; The housing further includes a second straight cylindrical section disposed below the conical section, wherein the inner diameter ratio of the light liquid phase discharge pipe to the second straight cylindrical section is 1.2-2.5:1; The hydrocyclone separator further includes a solvent backwash feed pipe disposed on the second straight section; The hydrocyclone separator is used to mix heavy oil and solvent and perform hydrocyclone separation to obtain a solvent-rich light liquid phase and a solid-rich heavy liquid phase. The solvent separation tower is used to separate the solvent-rich light liquid phase, and the resulting crude purified oil enters the first stripping tower for first stripping to obtain purified oil. The second stripping tower is used to perform a second stripping of the solid-rich heavy liquid phase, and the resulting solid residue is fed into the asphalt gasification furnace for oxidation reaction to obtain crude syngas.

21. The system according to claim 20, wherein, The system further includes: a heavy oil storage tank connected to the material feed pipe of the hydrocyclone separator, and a solvent storage tank connected to the solvent feed pipe of the hydrocyclone separator.

22. The system according to claim 21, wherein, The solvent storage tank is also connected to the solvent backwash feed pipe of the hydrocyclone separator.

23. The system according to claim 21, wherein, The top of the solvent separation tower, the top of the first stripping tower, and the top of the second stripping tower are each independently connected to the solvent storage tank, and are used to return the high-temperature solvent obtained from the solvent separation, the first stripping solvent obtained from the first stripping tower, and the second stripping solvent obtained from the second stripping tower to the solvent storage tank, respectively.

24. The system according to claim 21, wherein, The system further includes: an oil pump installed on the connecting pipeline between the heavy oil storage tank and the hydrocyclone, and a solvent pump installed on the connecting pipeline between the solvent storage tank and the hydrocyclone.

25. The system according to claim 20, wherein, The system further includes a catalytic hydrogenation unit connected to the first stripping tower, used to refine the purified oil to obtain refined oil products.

26. A method for processing heavy oil, characterized in that, The method is performed in the system according to any one of claims 20-25, wherein the method includes the following steps: (1) Mix heavy oil and solvent and perform hydrocyclone separation to obtain a solvent-rich light liquid phase and a solid-rich heavy liquid phase; (2) The solvent-rich light liquid phase is subjected to solvent separation, and the crude purified oil obtained is subjected to first stripping to obtain purified oil; (3) The solid-rich heavy liquid phase is subjected to a second stripping, and the resulting solid residue is subjected to an oxidation reaction to obtain crude syngas.

27. The method according to claim 26, wherein, The method further includes: independently returning and mixing the high-temperature solvent obtained from the solvent separation, the first stripping solvent obtained from the first stripping, and the second stripping solvent obtained from the second stripping into the solvent.

28. The method according to claim 26, wherein, The method further includes: refining the purified oil obtained in step (2) to obtain refined oil.

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