Asphaltene aggregating agent composition as well as preparation method and application thereof

Abstract

The invention discloses an asphaltene aggregating agent composition as well as a preparation method and application thereof. The aggregating agent composition comprises the following components in percentage by mass: 75-85 wt% of waste plastic; 5 wt% to 15 wt% of deoiled asphalt; 2 wt% to 10 wt% of kitchen waste oil; 2 wt% to 10 wt% of Tween-80; and 1 wt%-2 wt% of sulfonic acid. The asphaltene aggregating agent composition is suitable for producing deasphalted oil from petroleum residual oil, and the solvent deasphalting extraction quality and extraction efficiency are improved.

Description

Technical Field

[0001] The present invention belongs to the field of solvent deasphalting, and particularly relates to an asphaltene aggregator composition, a preparation method thereof, and an application thereof. Background Art

[0002] Petroleum asphaltene is the heaviest component in crude oil, with strong aromaticity and polarity. Aggregation is likely to occur during the refining process, which greatly hinders the processing and utilization of heavy oil. The main manifestations are as follows: First, petroleum asphaltene contains many acidic functional groups. Asphaltene aggregation will corrode pipelines and equipment. Second, petroleum asphaltene contains heteroatoms such as nitrogen and sulfur, as well as heavy metals such as vanadium and nickel. Their contents depend on the raw material source and mainly exist in the form of porphyrin complexes. They will poison the catalyst and reduce the activity of the catalyst. Third, petroleum asphaltene contains many polycyclic aromatic hydrocarbons. When heated at high temperature, polycyclic aromatic hydrocarbons are prone to coke formation, resulting in the blockage of reactors and pipelines.

[0003] The conventional asphaltene separation method is the SDA (solvent deasphalting) technology. SDA is a petrochemical refining process that separates substances from vacuum residue by extraction. Generally, light hydrocarbons such as propane, butane, and pentane are used as solvents. By using the different solubility of solvents for different components of vacuum residue, deasphalted oil (DAO) rich in saturated hydrocarbons is separated from vacuum residue, and at the same time, deoiled asphalt (DOA) rich in resins and asphaltenes is obtained.

[0004] SDA has the characteristics of simple process flow and strong raw material adaptability, and is a flexible residue pretreatment unit. However, with the increasing crude oil processing capacity in many refineries, the mismatch problem between the increasing processing volume of inferior resources such as vacuum residue and the processing capacity of the solvent deasphalting unit has become increasingly prominent. It is becoming increasingly important to develop a method that can improve the extraction efficiency and increase the processing capacity of the unit without adding external equipment and without changing the product quality between not expanding the solvent deasphalting capacity or building a solvent deasphalting unit with a larger processing volume.

[0005] In summary, for the problem of how to improve the extraction efficiency and quality in the solvent deasphalting process, the solutions in the prior art are rarely involved and need further research. Summary of the Invention

[0006] In view of the deficiencies of the solutions in the prior art, the present invention proposes a solution of adding an asphaltene aggregating agent to the petroleum resid, the feedstock for solvent deasphalting. By the interaction between the additive and the asphaltene in the petroleum resid, the aggregation of asphaltene in the petroleum resid is accelerated, so as to achieve the purpose of improving the extraction efficiency and quality. The problems such as improving the extraction efficiency of the device can be solved without expanding the capacity of solvent deasphalting and without changing the product quality. At the same time, the raw materials for preparing the aggregating agent mainly consist of waste plastics, deoiled asphalt from extraction residue and kitchen waste grease, realizing the resource utilization and high-value utilization of solid and liquid waste.

[0007] The present invention provides an asphaltene aggregating agent composition, a preparation method thereof and an application thereof. The asphaltene aggregating agent composition is applicable to the production of deasphalted oil from petroleum resid and improves the extraction efficiency and extraction quality.

[0008] In the first aspect of the present invention, an asphaltene aggregating agent composition is provided. The aggregating agent composition, in terms of mass fraction, includes:

[0009] 75 wt% to 85 wt% of waste plastics;

[0010] 5 wt% to 15 wt% of deoiled asphalt;

[0011] 2 wt% to 10 wt% of kitchen waste grease;

[0012] 2 wt% to 10 wt% of Tween-80;

[0013] 1 wt% to 2 wt% of sulfonic acid.

[0014] According to the present invention, the waste plastics are at least one of polypropylene resin, polyethylene resin, polyvinyl chloride resin, acrylonitrile-butadiene-styrene copolymer, and epoxy resin. The specific gravity of the waste plastics is 0.90 to 1.40 g·cm -3 .

[0015] According to the present invention, the mass content of the aromatic fraction in the deoiled asphalt is 25 wt% to 35 wt%. As a non-limiting example, the mass content of the aromatic fraction in the deoiled asphalt can be any value among 25 wt%, 27 wt%, 28 wt%, 29 wt%, 30 wt%, 32 wt%, etc.

[0016] According to the present invention, the water content of the kitchen waste grease is below 0.7 wt% by mass percentage.

[0017] In the second aspect of the present invention, a preparation method of the asphaltene aggregating agent composition is provided. The preparation method includes: uniformly mixing waste plastics, deoiled asphalt, kitchen waste grease, Tween-80, and sulfonic acid to obtain the asphaltene aggregating agent composition.

[0018] According to the present invention, in the preparation method of the asphaltene aggregating agent composition, waste plastics are crushed and melted and then mixed with other raw materials. Preferably, washing can be carried out before crushing. The washing solvent is water.

[0019] According to the present invention, in the preparation method of the asphaltene aggregating agent composition, the source of the deoiled asphalt is the heavy fraction obtained after the vacuum residue passes through a solvent deasphalting unit. The vacuum residue includes at least one of light sand, medium sand and heavy sand vacuum residues. Preferably, the solvent is butane. The operating conditions for solvent deasphalting are: the operating pressure is 4.0 MPa to 9.0 MPa, the operating temperature: the top of the column is 110 °C to 150 °C, the middle of the column is 105 °C to 140 °C, the bottom of the column is 100 °C to 140 °C, and the temperature decreases sequentially from top to bottom; the yield of the deoiled asphalt is controlled to be 40 wt% to 60 wt%. The mass content of the aromatic fraction of the deoiled asphalt is 25 wt% to 35 wt%. As a non-limiting example, the mass content of the aromatic fraction of the deoiled asphalt can be any value among 25 wt%, 27 wt%, 28 wt%, 29 wt%, 30 wt%, 32 wt%, etc.

[0020] According to the present invention, in the preparation method of the asphaltene aggregating agent composition, the mixing is carried out under stirring. Preferably, the stirring speed is 100 to 500 r / min. The pressure for mixing is 0.5 to 2 MPa. The temperature for mixing is 150 to 300 °C. The mixing time is 30 to 90 min. The mixing equipment is a reaction kettle.

[0021] The third aspect of the present invention provides the application of the asphaltene aggregating agent composition in the production of deasphalted oil.

[0022] According to the present invention, the method of the application includes: using petroleum resid as the feedstock oil; using an alkane solvent as the extractant; extracting the feedstock oil added with the aggregating agent composition with the extractant, and the obtained extract is the deasphalted oil.

[0023] According to the present invention, the petroleum resid is the residue obtained by the atmospheric or vacuum distillation of crude oil, preferably vacuum residue. The properties of the petroleum resid are: the mass content of asphaltene is 5 wt% to 12 wt%; the 10% distillation point ≥ 500 °C, preferably 500 to 530 °C; the heavy metal content is 100 to 400 mg / kg, where the heavy metals are counted as the total of Ni and V; the carbon residue value is 10 wt% to 25 wt%.

[0024] According to the present invention, the alkane solvent is an alkane with 3 to 5 carbon atoms. Preferably, the alkane solvent includes at least one of propane, butane and pentane, preferably butane.

[0025] According to the present invention, the addition amount of the aggregating agent composition accounts for 1.0 wt% to 8.0 wt%, preferably 1.0 wt% to 5.0 wt% of the mass of the petroleum residue. As a non-limiting example, the proportion of the addition amount of the aggregating agent in the mass of the petroleum residue can be 3 wt%, 4 wt%, 5 wt%, 6 wt%.

[0026] According to the present invention, the mass ratio of the alkane solvent to the petroleum residue (agent-oil ratio) is 3:1 to 8:1.

[0027] According to the present invention, the extraction process is preferably carried out in an extraction tower. The operating pressure of the extraction is 3.8 to 10.0 MPa. The extraction temperature is 50 to 190 °C. Preferably, a constant pressure and temperature reduction operation mode is adopted in the extraction tower. The temperature ranges at various parts of the extraction tower are as follows: 70 to 190 °C at the top of the tower, 60 to 180 °C in the middle of the tower, and 50 to 170 °C at the bottom of the tower. Preferably, it is 100 to 140 °C at the top of the tower, 90 to 130 °C in the middle of the tower, and 80 to 120 °C at the bottom of the tower. Preferably, the temperature at each part of the extraction tower: the temperature at the top of the tower is at least 10 to 30 °C higher than that in the middle of the tower; the temperature in the middle of the tower is at least 10 to 30 °C higher than that at the bottom of the tower.

[0028] According to the present invention, preferably, the feedstock oil can be preheated before entering the extraction tower. The feedstock oil is preheated to 100 to 180 °C.

[0029] According to the present invention, the operation process of the extraction is as follows: the extractant enters the tower from the bottom along with the solvent and flows upward, the petroleum residue enters the tower from the middle of the tower and flows downward, the petroleum residue and the extractant are in countercurrent contact in the tower, the residue is discharged from the bottom of the tower, and the extract is discharged from the upper part of the tower; the extract is the target product deasphalted oil.

[0030] Compared with the prior art, the beneficial effects of the present invention mainly include:

[0031] (1) In the asphaltene aggregating agent composition of the present invention, the aggregating agent composition, by mass fraction, includes: 75 wt% to 85 wt% of waste plastics; 5 wt% to 15 wt% of deoiled asphalt; 2 wt% to 10 wt% of kitchen waste grease; 2 wt% to 10 wt% of Tween-80; 1 wt% to 2 wt% of sulfonic acid. Waste plastics and deoiled asphalt are added to the aggregating agent composition. The waste plastics play a role in methylene bridging, and the deoiled asphalt plays a role in similar compatibility. Preferably, the content of aromatic components in the deoiled asphalt is further limited, which is beneficial to the aggregation of dispersed asphaltenes in the raw material. The components with specific compositions and contents in the composition cooperate with each other to play the best role. The asphaltene aggregating agent composition is applicable to the production of deasphalted oil from petroleum residue, improving the extraction efficiency and extraction quality.

[0032] (2) In the preparation method of the aggregating agent composition of the present invention, the method includes: uniformly mixing waste plastics, deoiled asphalt, kitchen waste oil and grease, Tween-80, and sulfonic acid to obtain an asphaltene aggregating agent composition. The aggregating agent composition prepared by this method is applicable to the production of deasphalted oil from petroleum residua.

[0033] (3) In the application of the asphaltene aggregating agent composition of the present invention, by adding a specific content of the aggregating agent composition to petroleum residua, the force of interaction is formed between the methylene chains in the aggregating agent composition and the feed vacuum residua, accelerating the aggregation of asphaltenes, achieving the improvement of the solvent deasphalting extraction quality and extraction efficiency without changing the internal components of the extraction column. In particular, while reducing the carbon residue value of the deasphalted oil, the heavy metal content is also reduced. Detailed implementation mode

[0034] The present invention will be further described in detail below in conjunction with examples, but the present invention is not limited to these examples.

[0035] In the present invention, the feedstock oil used in each example is vacuum residua. Its properties are as follows: the 10% distillation point is 530 °C, the asphaltene mass content is 5.4 wt%, the carbon residue value is 21.4 wt%, and the heavy metal content is 355.3 mg / kg, where the heavy metals are counted as the total of Ni and V.

[0036] In the present invention, the extraction efficiency = (the receiving rate of deasphalted oil / the feeding rate of residua) × 100%.

[0037] In the present invention, the carbon residue value is tested by the test method of GB / T 17144-1997 Determination of Carbon Residue of Petroleum Products.

[0038] In the present invention, the heavy metal content is tested by the test method of GB / T 37160-2019 Inductively Coupled Plasma Emission Spectrometry.

[0039] In the present invention, % is the mass percentage unless otherwise specified.

[0040] In the present invention, the water content of the kitchen waste oil and grease in each example is 0.4 wt%.

[0041] Example 1

[0042] The preparation method of the aggregating agent composition is as follows: 85 parts of waste polyethylene resin plastics with a specific gravity of 0.93 g·cm -3 are crushed and melted and added to the reaction kettle, and then 5 parts of deoiled asphalt with an aromatic content of 25 wt%, 7 parts of kitchen waste oil and grease, 2 parts of Tween-80, and 1 part of sulfonic acid are added in sequence. The heating temperature is 250 °C, the heating pressure is 2 MPa, and the stirring speed is 200 r / min. After reacting for 30 min, the aggregating agent composition is taken out.

[0043] The raw material vacuum residue is preheated to 100 °C and enters the solvent deasphalting unit (extraction column), with the residue feed rate being 2 kg / h. Butane is used as the solvent, and the solvent-to-oil ratio is 3:1. The aggregating agent composition is crushed into 80-mesh particles and slowly and evenly added to the vacuum residue. The addition amount of the aggregating agent composition accounts for 3 wt% of the mass of the raw material oil. The extraction conditions are: the operating pressure is 4.0 MPa, the top of the column is 120 °C, the middle of the column is 110 °C, and the bottom of the column is 100 °C. The receiving rate of the deasphalted oil is 1.12 kg / h. The carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 4.8 wt%, and the heavy metal content of the deasphalted oil is 32.6 mg / kg.

[0044] Example 2

[0045] The preparation method of the aggregating agent composition is as follows: Take waste polyethylene resin plastic with a specific gravity of 0.93 g·cm -3 82 parts are crushed and melted and added to the reaction kettle. Then, 8 parts of deoiled asphalt with an aromatic content of 25%, 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid are added in sequence. The heating temperature is 250 °C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, the aggregating agent composition is taken out.

[0046] The raw material vacuum residue is preheated to 100 °C and enters the solvent deasphalting unit (extraction column), with the residue feed rate being 2 kg / h. Butane is used as the solvent, and the solvent-to-oil ratio is 3:1. The aggregating agent composition is crushed into 80-mesh particles and slowly and evenly added to the vacuum residue. The addition amount accounts for 1% of the mass of the raw material oil. The extraction conditions are: the operating pressure is 4.0 MPa, the top of the column is 120 °C, the middle of the column is 110 °C, and the bottom of the column is 100 °C. The receiving rate of the deasphalted oil is 1.0 kg / h. The carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 5.1 wt%, and the heavy metal content of the deasphalted oil is 37.3 mg / kg.

[0047] Example 3

[0048] The preparation method of the aggregating agent composition is as follows: Take waste polyethylene resin plastic with a specific gravity of 0.93 g·cm -3 80 parts are crushed and melted and added to the reaction kettle. Then, 11 parts of deoiled asphalt with an aromatic content of 25%, 7 parts of kitchen waste oil, 3 parts of Tween-80, and 1 part of sulfonic acid are added in sequence. The heating temperature is 250 °C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, the aggregating agent composition is taken out.

[0049] The raw material vacuum residue is preheated to 100°C and enters the solvent deasphalting unit (extraction column) with a residue feed rate of 2 kg / h. Butane is used as the solvent with a solvent-to-oil ratio of 3:1. The aggregating agent composition is crushed into 80-mesh particles and slowly and evenly added to the vacuum residue, with the addition amount accounting for 1% of the mass of the raw material oil. The extraction conditions are: operating pressure of 4.0 MPa, top temperature of 120°C, middle temperature of 110°C, and bottom temperature of 100°C. The deasphalted oil collection rate is 0.92 kg / h. The carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 5.4 wt%, and the heavy metal content of the deasphalted oil is 39.4 mg / kg.

[0050] Example 4

[0051] The preparation method of the aggregating agent composition is as follows: Take 85 parts of waste polyvinyl chloride resin plastics, crush and melt them and add them to the reaction kettle. Then add 5 parts of deoiled asphalt with an aromatic content of 25%, 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid in sequence. The heating temperature is 250°C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, take it out to obtain the aggregating agent composition. -3 Take 85 parts of waste polyvinyl chloride resin plastics, crush and melt them and add them to the reaction kettle. Then add 5 parts of deoiled asphalt with an aromatic content of 25%, 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid in sequence. The heating temperature is 250°C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, take it out to obtain the aggregating agent composition.

[0052] The raw material vacuum residue is preheated to 100°C and enters the solvent deasphalting unit (extraction column) with a residue feed rate of 2 kg / h. Butane is used as the solvent with a solvent-to-oil ratio of 3:1. The aggregating agent composition is crushed into 80-mesh particles and slowly and evenly added to the vacuum residue, with the addition amount accounting for 1% of the mass of the raw material oil. The extraction conditions are: operating pressure of 4.5 MPa, top temperature of 120°C, middle temperature of 110°C, and bottom temperature of 100°C. The deasphalted oil collection rate is 1.04 kg / h. The carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 5.0 wt%, and the heavy metal content of the deasphalted oil is 35.1 mg / kg.

[0053] Example 5

[0054] The preparation method of the aggregating agent composition is as follows: Take 85 parts of waste polyethylene resin plastics, crush and melt them and add them to the reaction kettle. Then add 5 parts of deoiled asphalt with an aromatic content of 30%, 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid in sequence. The heating temperature is 250°C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, take it out to obtain the aggregating agent composition. -3 Take 85 parts of waste polyethylene resin plastics, crush and melt them and add them to the reaction kettle. Then add 5 parts of deoiled asphalt with an aromatic content of 30%, 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid in sequence. The heating temperature is 250°C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, take it out to obtain the aggregating agent composition.

[0055] The vacuum residue of the feedstock oil is preheated to 100 °C and enters the solvent deasphalting unit (extraction column), and the residue oil feed rate is 2 kg / h. Butane is used as the solvent, and the solvent-to-oil ratio is 3:1. The aggregating agent composition is crushed into 80-mesh particles and slowly and evenly added to the vacuum residue oil, and the addition amount accounts for 1% of the mass of the feedstock oil. The extraction conditions are: the operating pressure is 4.5 MPa, the top of the column is 120 °C, the middle of the column is 110 °C, and the bottom of the column is 100 °C. The receiving rate of the deasphalted oil is 0.86 kg / h, and the carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 5.8 wt%, and the heavy metal content of the deasphalted oil is 40.0 mg / kg.

[0056] Comparative Example 1

[0057] The difference from Example 1 is that the aggregating agent composition is not added.

[0058] The vacuum residue of the feedstock oil is preheated to 100 °C and enters the solvent deasphalting unit (extraction column), and the residue oil feed rate is 2 kg / h. Butane is used as the solvent, and the solvent-to-oil ratio is 3:1. The extraction conditions are: the operating pressure is 4.0 MPa, the top of the column is 120 °C, the middle of the column is 110 °C, and the bottom of the column is 100 °C. The receiving rate of the deasphalted oil is 0.74 kg / h, and the carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 6.5 wt%, and the heavy metal content of the deasphalted oil is 48.3 mg / kg.

[0059] Comparative Example 2

[0060] The difference from Example 5 is that the de-oiled asphalt is not added to the aggregating agent composition.

[0061] The preparation method of the aggregating agent composition is as follows: 85 parts of waste polyethylene resin plastics with a specific gravity of 1.35 g·cm -3 are crushed and melted and added to the reaction kettle, and 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid are added in sequence. The heating temperature is 250 °C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, it is taken out to obtain the aggregating agent composition.

[0062] The vacuum residue of the feedstock oil is preheated to 100 °C and enters the solvent deasphalting unit (extraction column), and the residue oil feed rate is 2 kg / h. Butane is used as the solvent, and the solvent-to-oil ratio is 3:1. The aggregating agent composition is crushed into 80-mesh particles and slowly and evenly added to the vacuum residue oil, and the addition amount accounts for 1% of the mass of the feedstock oil. The extraction conditions are: the operating pressure is 4.5 MPa, the top of the column is 120 °C, the middle of the column is 110 °C, and the bottom of the column is 100 °C. The receiving rate of the deasphalted oil is 0.78 kg / h, and the carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 6.2 wt%, and the heavy metal content of the deasphalted oil is 45.0 mg / kg.

[0063] Comparative Example 3

[0064] Same as Example 5, except that waste plastics are not added to the aggregating agent composition.

[0065] The preparation method of the aggregating agent composition is as follows: Take 5 parts of deoiled asphalt with an aromatic content of 30%, 7 parts of kitchen waste oil, 2 parts of Tween-80, and 1 part of sulfonic acid, and add them to the reaction kettle in sequence. The heating temperature is 250 °C, the pressure is 2 MPa, the stirring speed is 200 r / min, and after reacting for 30 min, take out to obtain the aggregating agent composition.

[0066] Preheat the raw material vacuum residue to 100 °C and enter the solvent deasphalting unit (extraction tower), and the residue feed rate is 2 kg / h. Butane is used as the solvent, and the solvent / oil ratio is 3:1. Crush the aggregating agent composition into 80-mesh particles, and slowly and evenly add it to the vacuum residue. The addition amount accounts for 1% of the mass of the raw material oil. The extraction conditions are: the operating pressure is 4.5 MPa, the top of the tower is 120 °C, the middle of the tower is 110 °C, and the bottom of the tower is 100 °C. The receiving rate of the deasphalted oil is 0.76 kg / h, and the carbon residue value and heavy metal content of the deasphalted oil are measured. The carbon residue value of the deasphalted oil fraction is 6.4 wt%, and the heavy metal content of the deasphalted oil is 45.6 mg / kg.

[0067] The specific embodiments of the present invention have been described in detail above. However, the present invention is not limited thereto. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, including any other suitable combination of each technical feature. These simple modifications and combinations should also be regarded as the content disclosed by the present invention and fall within the protection scope of the present invention.

Claims

1. An asphaltene aggregating agent composition, by mass fraction, comprising: 75wt% - 85wt% of waste plastics; 5wt% - 15wt% of deoiled asphalt; 2wt% - 10wt% of kitchen waste grease; 2wt% - 10wt% of Tween - 80; 1wt% - 2wt% of sulfonic acid.

2. The composition according to claim 1, wherein The waste plastics are at least one of polypropylene resin, polyethylene resin, polyvinyl chloride resin, acrylonitrile - butadiene - styrene copolymer, and epoxy resin.

3. The composition according to claim 1, wherein The specific gravity of the waste plastics is 0.90 to 1.40 g / cm -3 .

4. The composition according to claim 1, wherein The mass content of aromatic components in the deoiled asphalt is 25wt% - 35wt%.

5. A method for preparing the composition according to any one of claims 1 to 4, comprising: Mix the waste plastics, deoiled asphalt, kitchen waste grease, Tween - 80, and sulfonic acid evenly to obtain the asphaltene aggregating agent composition.

6. The method according to claim 5, characterized in that, The source of the deoiled asphalt is the heavy fraction obtained after the vacuum residue passes through a solvent deasphalting unit.

7. The method according to claim 5, characterized in that, The mixing is carried out under stirring; preferably, the stirring speed is 100 - 500r / min; and / or, the pressure of mixing is 0.5 - 1MPa; and / or, the temperature of mixing is 150 - 300°C; the mixing time is 30 - 90min.

8. Use of the asphaltene aggregating agent composition according to any one of claims 1 - 4 or prepared by the preparation method according to any one of claims 5 - 7 in the production of deasphalted oil.

9. The application according to claim 8, characterized in that The method of the use includes: using petroleum residue as the feedstock oil; using an alkane solvent as the extractant; extracting the feedstock oil added with the aggregating agent composition with the extractant, and the obtained extract is the deasphalted oil.

10. The application according to claim 9, characterized in that, The properties of the petroleum residue are: the mass content of asphaltene is 5wt% - 12wt%; the 10% distillation point ≥ 500°C, preferably 500 - 530°C; the heavy metal content is 100 - 400mg / kg, where the heavy metals are calculated as the total of Ni and V; the carbon residue value is 10wt% - 25wt%.