Preparation method of heavy traffic road asphalt

Abstract

The invention discloses a preparation method of heavy traffic road asphalt, which comprises the following steps: (1) catalytic cracking oil slurry passes through an oil slurry solid removal unit to obtain clarified oil slurry and high-solid oil slurry; (2) separating the clarified oil slurry and heavy oil in a solvent deasphalting unit to obtain an alkane-rich component, an aromatic hydrocarbon-rich component and deoiled asphalt; and (3) removing the solvent from the high-solid oil slurry and the deoiled asphalt in an asphalt gas stripping unit to obtain the heavy traffic road asphalt. According to the method, the standards of asphalt products with different brands in the national standard GB / T 15180-2010 can be directly obtained by adjusting process parameters, meanwhile, waste utilization of the high-solid oil slurry is realized, the preparation cost of the heavy-duty road asphalt is greatly reduced, and meanwhile, the alkane-rich component and the aromatic hydrocarbon-rich component of high-added-value products are obtained.

Description

Technical Field

[0001] The present invention relates to the field of petrochemical engineering, and particularly to a method for preparing heavy traffic road asphalt. Background Art

[0002] Asphalt is an indispensable material for constructing high-grade road surfaces. With the rapid growth of the total mileage of expressways globally, the demand for asphalt, especially for high-grade heavy traffic asphalt, is increasing. At the same time, countries around the world are introducing new standards for high-grade heavy traffic asphalt, and the index requirements for high-grade heavy traffic asphalt are constantly increasing. To address the problem of the continuous heavy quality of crude oil and to meet the basic requirements of the new standards, it is urgent to develop new processes for producing heavy traffic asphalt.

[0003] The process of producing asphalt by blending occupies an important position in the world's asphalt production processes. Producing asphalt by blending means adjusting the proportion between asphalt components according to the requirements of asphalt quality or colloidal structure to obtain products that can meet the usage requirements. However, this process requires repeated heating and is not easily mixed evenly. Moreover, with the continuous heavy quality and inferiority of crude oil properties, the solvent deasphalting technology aimed at optimizing catalytic cracking feedstock has developed significantly in China. This technology produces a part of deoiled asphalt with a high softening point and a small penetration. Since the deoiled asphalt has very little oil content and its penetration and ductility are almost zero, its properties are very different from the quality indicators of road asphalt and it cannot be directly utilized.

[0004] Catalytic slurry is cracked heavy oil obtained from fossil fuel petroleum and is a low-value by-product. Currently, refineries often use the externally discharged slurry as a blending oil for fuel oil or as a feedstock for delayed coking and sell it at a low price. Although the outlet of the slurry is temporarily solved, due to the large amount of aromatic components contained in the slurry, it causes waste of resources; moreover, the large amount of micron-sized catalyst particles contained in the catalytic slurry will cause serious pollution to the environment when burned as fuel.

[0005] Therefore, how to rationally utilize high-solid-content and low-value catalytic slurry and heavy oil to obtain heavy traffic road petroleum asphalt and clean aromatic-rich oil is of great strategic significance for the national economy and the green and low-carbon development of society. Summary of the Invention

[0006] The object of the present invention is to provide a method for preparing heavy traffic road asphalt. This method can obtain asphalt products that meet the technical requirements of heavy traffic road petroleum asphalt in GB / T 15180-2010, such as AH-130, AH-110, AH-90, AH-70, AH-50, or AH-30, by adjusting process parameters. At the same time, high-value-added and high-quality aromatic-rich components and alkane-rich components are obtained.

[0007] To achieve the above object, the present invention provides the following technical solutions:

[0008] A preparation method of heavy traffic road asphalt, comprising the following steps:

[0009] (1) The catalytic cracking slurry passes through the slurry solid removal unit and is separated at high temperature to obtain clarified slurry and high-solid slurry (containing large particle size solid particles);

[0010] (2) The clarified slurry and heavy oil are separated in the solvent deasphalting unit, and through extraction separation, an alkane-rich component, an aromatic-rich component and deoiled asphalt are obtained respectively;

[0011] (3) After the high-solid slurry and the deoiled asphalt are stripped of the solvent in the asphalt stripping unit, heavy traffic road asphalt is directly obtained, improving the added value of the high-solid slurry.

[0012] In the prior art, most of the high-solid slurry obtained from the catalytic cracking slurry through the slurry solid removal unit is treated as waste liquid. Due to the characteristics of high solid content, poor stability and easy stratification during long-term static storage in the high-solid slurry, it causes difficulties in its processing and utilization. In the existing process of blending asphalt, the deoiled asphalt after stripping and the high-solid slurry are often stirred and blended. Therefore, when using the existing blending method to prepare heavy traffic road asphalt, the blended asphalt products generally have the phenomenon of unevenness, resulting in poor product stability and service performance, especially in terms of penetration and ductility, etc., the phenomenon of non-compliance will occur. In the present invention, the hot high-solid slurry with on-line solid removal and the deoiled asphalt without solvent stripping are mixed and fed into the asphalt stripping tower. Under the action of stripping and the removal of the solvent from the inside of the deoiled asphalt, the high-solid slurry with lower viscosity flows to the solvent removal part and is fully mixed with the deoiled asphalt by relying on the stripping gas flow. Finally, the well-mixed heavy traffic road petroleum asphalt product can be discharged from the tower. Moreover, this method can obtain asphalt products that meet the technical requirements of heavy traffic road petroleum asphalt in GB / T15180-2010, such as AH-130, AH-110, AH-90, AH-70, AH-50, or AH-30. At the same time, alkane-rich components and aromatic-rich components with high added value and high quality are obtained.

[0013] Optionally, the density (20°C) of the catalytic cracking slurry is 0.95 - 1.1 g / cm 3 , the ash content is 0.021 - 0.110%, and the solid content is 2000 - 7000 ppm.

[0014] Optionally, the solid content of the clarified slurry is 0 - 200 ppm.

[0015] Optionally, the mass ratio of the clarified slurry to the heavy oil is not specifically limited and can be adjusted according to actual situations and requirements. The recommended mass ratio of the clarified slurry to the heavy oil in the present invention is 1:1 to 20, such as 1:2, 1:3, 1:5, 1:8, 1:10, 1:12, 1:15, 1:17, 1:19, etc.

[0016] Optionally, the slurry solid removal unit includes a filtration buffer tank, a high-temperature slurry pump, and a membrane filter that are connected in sequence. The catalytic cracking slurry from the catalytic fractionation tower enters the filtration buffer tank and then enters the membrane filter through the high-temperature slurry pump for solid-liquid separation to remove most of the solid particles, obtaining the clarified slurry; the membrane filter includes 1 group of metal membranes or 2 to 3 groups of metal membranes connected in series;

[0017] The filtration temperature of the membrane filter is 70 to 200 °C.

[0018] Optionally, the heavy oil is selected from at least one of vacuum residue of naphthenic crude oil, vacuum residue of intermediate crude oil, and oil sand asphalt, etc.

[0019] Optionally, the solvent deasphalting unit includes an extraction column, a dearomatization column, an alkane stripping column, an aromatic stripping column, and a solvent recovery column. The clarified slurry buffer tank and the heavy oil buffer tank are respectively connected to the extraction column through a clarified slurry and heavy oil mixer.

[0020] Optionally, the rich alkane component, the rich aromatic component, and the deoiled asphalt are respectively obtained at the bottoms of the alkane stripping column, the aromatic stripping column, and the extraction column;

[0021] Preferably, the pressures of the extraction column, the dearomatization column, and the solvent recovery column are 4.0 to 5.0 MPa, and the pressures of the alkane stripping column and the aromatic stripping column are 0.5 to 1.0 MPa.

[0022] The clarified slurry from the slurry de-solidification unit enters the clarified slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. The clarified slurry and the heavy oil are intensively mixed in the clarified slurry and heavy oil mixer by their respective feed pumps. The mixed oil product enters the extraction column and makes full contact with the solvent in the extraction column for extraction. The de-oiled asphalt obtained at the bottom of the extraction column enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvents enter the de-aromatization column from the top of the extraction column. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization column. The alkane components and part of the solvent enter the alkane stripping column from the top of the de-aromatization column, and rich alkane components are obtained from the bottom of the alkane stripping column; the aromatic components and part of the solvent enter the aromatic stripping column from the bottom of the de-aromatization column, and rich aromatic components are obtained from the bottom of the aromatic stripping column; the solvent separated from the top of the alkane stripping column and the aromatic stripping column enters the solvent recovery column, and the recovered solvent is circulated to the extraction column and the de-aromatization column respectively from the top of the solvent recovery column.

[0023] Optionally, the solvent used in the extraction column and the de-aromatization column in the solvent deasphalting unit is selected from alkanes with C3-C5, preferably at least one of propane, n-butane, and isobutane.

[0024] Optionally, the asphalt stripping unit includes a feed mixer and an asphalt stripping column; the high-solid slurry and the de-oiled asphalt obtained at the bottom of the extraction column are mixed in the feed mixer and then enter the asphalt stripping column for stripping. The solvent obtained by stripping is circulated to the solvent recovery column, and the heavy traffic road asphalt product directly obtained at the bottom of the stripping column meets the standards of AH-130, AH-110, AH-90, AH-70, AH-50, and AH-30 in GB / T 15180-2010 (specifically, the asphalt products meeting different grades can be obtained by adjusting process parameters);

[0025] The pressure of the asphalt stripping column is controlled at 0.3 - 1.2 Mpa, and the temperature is controlled at 110 - 250 °C.

[0026] Optionally, the method for preparing heavy traffic road asphalt provided by the present invention further includes the step of sending the rich aromatic components into a deep purification unit for deep purification to obtain purified rich aromatic oil. The deep purification unit includes an oil filter and a hydrofining reactor connected in sequence; the purpose of using the oil filter for filtration is to remove the impurities introduced in the heavy oil, and then remove the fine particles and impurity sulfur contained in the hydrofining reactor; the solid content of the obtained purified rich aromatic oil is 0 - 20 ppm, and the sulfur content is less than 0.5 wt%.

[0027] Compared with the prior art, the present invention has the following advantages:

[0028] The preparation method of heavy traffic road asphalt provided by the present invention is a process for preparing heavy traffic road asphalt and aromatic-rich oil from catalytic cracking slurry and heavy oil. The catalytic cracking slurry enters the slurry solid removal unit, and clarified slurry and high-solid slurry are separated at high temperature. The clarified slurry is mixed with heavy oil and enters the solvent deasphalting unit, and alkane-rich components, aromatic-rich components and deoiled asphalt are separated through a two-stage extraction tower. The high-solid slurry is mixed with deoiled asphalt and enters the asphalt stripping unit, and the heavy traffic road asphalt product is directly obtained after removing the solvent. Specifically, asphalt products meeting the standards of AH-130, AH-110, AH-90, AH-70, AH-50 or AH-30 can be directly obtained by adjusting process parameters. At the same time, the waste utilization of high-solid slurry is realized, the preparation cost of heavy traffic road asphalt is greatly reduced, and high-value-added products, namely alkane-rich components and aromatic-rich components, are obtained. By further purifying the aromatic-rich components obtained after the two-stage extraction tower in a deep purification unit, a clean and aromatic-rich oil product is obtained.

[0029] The preparation method of heavy traffic road asphalt provided by the present invention effectively solves the problem that the high-solid-content slurry cannot be utilized after slurry solid removal. The high-solid slurry and deoiled asphalt are mixed and synergistically enter the asphalt stripping unit, reducing the viscosity of the oil product, reducing the stripping load, and directly obtaining the heavy traffic road asphalt product, reducing the dosage of the original deoiled asphalt components, reducing the production cost of asphalt, and increasing the added value of the high-solid slurry. Mixing the clarified slurry after slurry solid removal with heavy oil reduces the viscosity of the solvent deasphalting raw material, increases the content of low-solid-content, high-value-added and high-quality aromatic-rich components in the product, and obtains aromatic-rich oil after deep purification, which can be used as a raw material in the field of carbon materials, overall improving the utilization rate and economy of catalytic cracking slurry. The slurry and heavy oil are processed centrally once to prepare two important products, namely heavy traffic road asphalt and aromatic-rich oil. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 is a flow chart of the preparation method of heavy traffic road asphalt provided by the present invention;

[0031] Figure 2 is a flow chart of the solvent deasphalting unit in the preparation method of heavy traffic road asphalt provided by the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0032] The present invention will be specifically described below through examples. It is necessary to point out here that the following examples are only used to further illustrate the present invention and cannot be understood as limiting the protection scope of the present invention. Those skilled in the art can make some non-essential improvements and adjustments to the present invention according to the above content of the present invention.

[0033] For those examples where specific experimental procedures or conditions are not specified, the operations or conditions of the conventional experimental procedures described in the literature in this field can be followed. For reagents or instruments whose manufacturers are not specified, they are all conventional reagent products that can be obtained through commercial purchase.

[0034] Example 1

[0035] This example provides a preparation method for heavy traffic road asphalt, as Figure 1 shown, including the following steps:

[0036] (1) The catalytic cracking slurry with a density (at 20 °C) of 0.98 g / cm 3 , an ash content of 0.080%, and a solid content of 2500 ppm is fed from the filtration buffer tank into the membrane filter (using 1 set of metal membranes) by a high-temperature slurry pump for separation at 80 °C to obtain clarified slurry (with a solid content of 20 ppm) and high-solid slurry;

[0037] (2) The vacuum residue of naphthenic Liaohe crude oil is selected as the heavy oil. The above-mentioned clarified slurry is mixed with this heavy oil in a mass ratio of 1:1 and enters the solvent deasphalting unit (as Figure 2 shown). Specifically, the clarified slurry from the slurry solid removal unit enters the clarified slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. They are strongly mixed in the clarified slurry and heavy oil mixer by their respective feed pumps. The mixed oil product enters the extraction column and comes into full contact with the solvent in the extraction column for extraction. The deoiled asphalt obtained at the bottom of the extraction column enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvents enter the de-aromatization column from the top of the extraction column. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization column. Among them, the alkane components and part of the solvent enter the alkane stripping column from the top of the de-aromatization column, and the alkane-rich components are obtained from the bottom of the alkane stripping column; the aromatic components and part of the solvent enter the aromatic stripping column from the bottom of the de-aromatization column, and the aromatic-rich components are obtained from the bottom of the aromatic stripping column; the solvent separated from the tops of the alkane stripping column and the aromatic stripping column enters the solvent recovery column, and the recovered solvent is circulated to the extraction column and the de-aromatization column respectively from the top of the solvent recovery column.

[0038] Among them, propane is used as the solvent. The pressure of the extraction column is controlled at 4.0 Mpa, the pressure of the de-aromatization column is controlled at 4.2 Mpa, the pressure of the alkane stripping column is controlled at 0.6 Mpa, the pressure of the aromatic stripping column is 0.6 MPa, and the pressure of the solvent recovery column is 4.2 Mpa.

[0039] (3) The high-solid slurry and the deoiled asphalt are mixed in the feed mixer and then enter the asphalt stripping column. The pressure of the asphalt stripping column is controlled at 0.6 MPa and the temperature is at 150 °C. The penetration of the asphalt product obtained after removing the solvent is 128 dmm, and the softening point is 42 °C, meeting the requirements of the AH-130 heavy traffic road asphalt product.

[0040] (4) The rich aromatic component obtained at the bottom of the de-aromatization tower is filtered successively through an oil filter to remove the impurities introduced in the heavy oil, and then the fine particles and impurity sulfur contained are removed by hydrotreating in a hydrofining reactor to obtain a rich aromatic oil product with a solid content of 8 ppm and a sulfur content of 0.344%.

[0041] Example 2

[0042] This example provides a method for preparing heavy traffic road asphalt, as Figure 1 shown, including the following steps:

[0043] (1) The catalytic cracking slurry with a density (at 20 °C) of 0.95 g / cm 3 , an ash content of 0.020%, and a solid content of 2000 ppm is fed from the filtration buffer tank into a membrane filter (using 1 set of metal membranes) by a high-temperature slurry pump for separation at 70 °C to obtain a clarified slurry (with a solid content of 16 ppm) and a high-solid slurry;

[0044] (2) The vacuum residue of the intermediate-based Zakum crude oil is selected as the heavy oil, and the above-mentioned clarified slurry is mixed with the heavy oil in a mass ratio of 1:2 and fed into the solvent deasphalting unit (as Figure 2 shown). Specifically, the clarified slurry from the oil slurry solid removal unit enters the clarified slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. The two are strongly mixed in a clarified slurry and heavy oil mixer by their respective feed pumps, and the mixed oil product enters the extraction tower to fully contact and extract with the solvent in the extraction tower. The deoiled asphalt obtained at the bottom of the extraction tower enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvents enter the de-aromatization tower from the top of the extraction tower. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization tower. The alkane components and solvents enter the alkane stripping tower from the top of the de-aromatization tower, and a rich alkane component is obtained from the bottom of the alkane stripping tower; the aromatic components and solvents enter the aromatic stripping tower from the bottom of the de-aromatization tower, and a rich aromatic component is obtained from the bottom of the aromatic stripping tower; the solvents separated from the tops of the alkane stripping tower and the aromatic stripping tower enter the solvent recovery tower, and the recovered solvents are respectively recycled from the top of the solvent recovery tower to the extraction tower and the de-aromatization tower.

[0045] Among them, the solvent is a mixture of propane and n-butane in a mass ratio of 1:1. The pressure of the extraction tower is controlled at 4.1 Mpa, the pressure of the de-aromatization tower is controlled at 4.3 Mpa, the pressure of the alkane stripping tower is controlled at 0.5 Mpa, the pressure of the aromatic stripping tower is 0.5 MPa, and the pressure of the solvent recovery tower is 4.3 Mpa.

[0046] (3) Mix the high-solid oil slurry and deoiled asphalt in a feed mixer and then enter the asphalt stripping column. Control the pressure of the asphalt stripping column at 0.3 MPa and the temperature at 110 °C. The penetration of the asphalt product obtained after removing the solvent is 128 dmm, and the softening point is 43 °C, meeting the requirements of the heavy traffic road asphalt product of AH-110;

[0047] (4) Filter the aromatic-rich components obtained at the bottom of the de-aromatization column successively through an oil filter to remove the impurities introduced in the heavy oil. Then, remove the fine particles and impurity sulfur contained through hydrotreating in a hydrofining reactor to obtain an aromatic-rich oil product with a solid content of 2 ppm and a sulfur content of 0.274%.

[0048] Example 3

[0049] This example provides a preparation method for heavy traffic road asphalt, as Figure 1 shown, including the following steps:

[0050] (1) Feed the catalytic cracking oil slurry with a density (20 °C) of 0.99 g / cm 3 , an ash content of 0.080%, and a solid content of 6500 ppm into a membrane filter (using 2 groups of metal membranes in series) from a filtration buffer tank through a high-temperature oil slurry pump for separation at 180 °C to obtain clarified oil slurry (with a solid content of 147 ppm) and high-solid oil slurry;

[0051] (2) Select the vacuum residue of intermediate-base Basrah crude oil as the heavy oil. Mix the above-mentioned clarified oil slurry and the heavy oil in a mass ratio of 1:10 and enter the solvent deasphalting unit (as Figure 2 shown). Specifically, the clarified oil slurry from the oil slurry solid removal unit enters the clarified oil slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. They are intensively mixed in a clarified oil slurry and heavy oil mixer through their respective feed pumps. The mixed oil product enters the extraction column and comes into full contact with the solvent in the extraction column for extraction. The deoiled asphalt obtained at the bottom of the extraction column enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvents enter the de-aromatization column from the top of the extraction column. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization column. The alkane components and solvents enter the alkane stripping column from the top of the de-aromatization column, and the alkane-rich components are obtained from the bottom of the alkane stripping column; the aromatic components and solvents enter the aromatic stripping column from the bottom of the de-aromatization column, and the aromatic-rich components are obtained from the bottom of the aromatic stripping column; the solvents separated from the tops of the alkane stripping column and the aromatic stripping column enter the solvent recovery column, and the recovered solvents are respectively recycled to the extraction column and the de-aromatization column from the top of the solvent recovery column.

[0052] Among them, the solvent is n-butane. The pressure of the extraction column is controlled at 4.3 Mpa, the pressure of the de-aromatization column is controlled at 4.5 Mpa, the pressure of the alkane stripping column is controlled at 0.7 Mpa, the pressure of the aromatic stripping column is 0.7 MPa, and the pressure of the solvent recovery column is 4.5 Mpa.

[0053] (3) Mix the high-solid oil slurry and the deoiled asphalt in the feed mixer and then enter the asphalt stripping column. Control the pressure of the asphalt stripping column at 0.8 MPa and the temperature at 150 °C. The penetration of the asphalt product obtained after removing the solvent is 92 dmm, and the softening point is 46 °C, meeting the requirements of the heavy traffic road asphalt product of AH-90;

[0054] (4) Filter the rich aromatic components obtained at the bottom of the de-aromatization column through an oil filter in sequence to remove the impurities introduced in the heavy oil, and then remove the fine particles and impurity sulfur contained through hydrotreating in a hydrofining reactor to obtain a rich aromatic oil product with a solid content of 17 ppm and a sulfur content of 0.419%.

[0055] Example 4

[0056] This example provides a method for preparing heavy traffic road asphalt, as Figure 1 shown, including the following steps:

[0057] (1) Feed the catalytic cracking oil slurry with a density (20 °C) of 0.96 g / cm 3 , an ash content of 0.11%, and a solid content of 7000 ppm into the membrane filter (using 2 groups of metal membranes in series) from the filtration buffer tank through a high-temperature oil slurry pump for separation at 200 °C to obtain clarified oil slurry (solid content of 192 ppm) and high-solid oil slurry;

[0058] (2) Select intermediate-base Kuwait vacuum residue as the heavy oil, and mix the above-mentioned clarified oil slurry and the heavy oil in a mass ratio of 1:8 and enter the solvent deasphalting unit (as Figure 2As shown in the figure, specifically, the clarified slurry from the slurry de-solidification unit enters the clarified slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. The clarified slurry and heavy oil are strongly mixed in the clarified slurry and heavy oil mixer by their respective feed pumps. The mixed oil product enters the extraction column and is in full contact with the solvent in the extraction column for extraction. The de-oiled asphalt obtained at the bottom of the extraction column enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvent enter the de-aromatization column from the top of the extraction column. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization column. The alkane components and solvent enter the alkane stripping column from the top of the de-aromatization column, and the alkane-rich components are obtained from the bottom of the alkane stripping column; the aromatic components and solvent enter the aromatic stripping column from the bottom of the de-aromatization column, and the aromatic-rich components are obtained from the bottom of the aromatic stripping column; the solvent separated from the top of the alkane stripping column and the aromatic stripping column enters the solvent recovery column, and the recovered solvent is respectively recycled to the extraction column and the de-aromatization column from the top of the solvent recovery column.

[0059] Among them, the solvent is a mixture of pentane and n-butane with a mass ratio of 1:1. The pressure of the extraction column is controlled at 4.0 Mpa, the pressure of the de-aromatization column is controlled at 5 Mpa, the pressure of the alkane stripping column is controlled at 0.8 Mpa, the pressure of the aromatic stripping column is 0.8 MPa, and the pressure of the solvent recovery column is 5 Mpa.

[0060] (3) Mix the high-solid slurry and de-oiled asphalt in the feed mixer and then enter the asphalt stripping column. Control the pressure of the asphalt stripping column at 1.0 MPa and the temperature at 180 °C. The penetration of the asphalt product obtained after removing the solvent is 64 dmm, and the softening point is 50 °C, meeting the requirements of the AH-70 heavy traffic road asphalt product.

[0061] (4) The aromatic-rich components obtained at the bottom of the de-aromatization column are filtered through an oil filter in sequence to remove the impurities introduced in the heavy oil, and then the fine particles and impurity sulfur contained are removed by hydrotreating in a hydrofining reactor to obtain an aromatic-rich oil product with a solid content of 18 ppm and a sulfur content of 0.366%.

[0062] Example 5

[0063] This example provides a method for preparing heavy traffic road asphalt, as Figure 1 shown, including the following steps:

[0064] (1) The catalytic cracking slurry with a density (20 °C) of 1.03 g / cm 3 , an ash content of 0.075%, and a solid content of 4600 ppm is pumped from the filtration buffer tank into the membrane filter (using 2 groups of metal membranes in series) by a high-temperature slurry pump for separation at 160 °C to obtain clarified slurry (solid content of 108 ppm) and high-solid slurry;

[0065] (2) Select Canadian oil sand asphalt as heavy oil, and mix the above clarified slurry with this heavy oil at a mass ratio of 1:16 and enter the solvent deasphalting unit (as shown in Figure 2 ), specifically, the clarified slurry from the slurry solid removal unit enters the clarified slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. The clarified slurry and the heavy oil are intensively mixed in the clarified slurry and heavy oil mixer by their respective feed pumps. The mixed oil product enters the extraction column and makes full contact with the solvent in the extraction column for extraction. The deoiled asphalt obtained at the bottom of the extraction column enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvents enter the de-aromatization column from the top of the extraction column. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization column. The alkane components and solvents enter the alkane stripping column from the top of the de-aromatization column, and rich alkane components are obtained from the bottom of the alkane stripping column; the aromatic components and solvents enter the aromatic stripping column from the bottom of the de-aromatization column, and rich aromatic components are obtained from the bottom of the aromatic stripping column; the solvents separated from the tops of the alkane stripping column and the aromatic stripping column enter the solvent recovery column, and the recovered solvents are respectively recycled to the extraction column and the de-aromatization column from the top of the solvent recovery column.

[0066] Among them, the solvent uses a mixture of pentane and n-butane at a mass ratio of 1:2. The pressure of the extraction column is controlled at 4.3 Mpa, the pressure of the de-aromatization column is controlled at 4.5 Mpa, the pressure of the alkane stripping column is controlled at 1 Mpa, the pressure of the aromatic stripping column is 1 MPa, and the pressure of the solvent recovery column is 4.5 Mpa.

[0067] (3) Mix the high-solid slurry and the deoiled asphalt in the feed mixer and then enter the asphalt stripping column. Control the pressure of the asphalt stripping column at 1.2 MPa and the temperature at 250 °C. The penetration of the asphalt product obtained after removing the solvent is 54 dmm, and the softening point is 52 °C, meeting the requirements of the AH-50 heavy traffic road asphalt product;

[0068] (4) The rich aromatic components obtained at the bottom of the de-aromatization column are filtered through an oil filter in sequence to remove the impurities introduced in the heavy oil, and then the fine particles and impurity sulfur contained are removed by hydrotreating in a hydrofining reactor to obtain a rich aromatic oil product with a solid content of 18 ppm and a sulfur content of 0.366%.

[0069] Example 6

[0070] This example provides a preparation method of heavy traffic road asphalt, as shown in Figure 1 , including the following steps:

[0071] (1) The density (20 °C) is 1.1 g / cm 3, the catalytic cracking slurry with an ash content of 0.097% and a solid content of 6700 ppm enters the membrane filter (with 3 groups of metal membranes in series) from the filtration buffer tank through a high-temperature slurry pump and is separated at 180 °C to obtain clarified slurry (with a solid content of 132 ppm) and high-solid slurry;

[0072] (2) Select Canadian oil sand asphalt as heavy oil. Mix the above-mentioned clarified slurry with the heavy oil in a mass ratio of 1:20 and enter the solvent deasphalting unit (as Figure 2 shown). Specifically, the clarified slurry from the slurry solid removal unit enters the clarified slurry buffer tank, and the heavy oil is in the heavy oil buffer tank. The clarified slurry and the heavy oil are intensively mixed in the clarified slurry and heavy oil mixer by their respective feed pumps. The mixed oil product enters the extraction column and is in full contact with the solvent in the extraction column for extraction. The deoiled asphalt obtained at the bottom of the extraction column enters the subsequent asphalt stripping unit. Light components such as aromatics, non-aromatics, and solvents enter the de-aromatization column from the top of the extraction column. The light components are further extracted and separated into alkane components and aromatic components in the de-aromatization column. The alkane components and solvents enter the alkane stripping column from the top of the de-aromatization column, and rich alkane components are obtained from the bottom of the alkane stripping column; the aromatic components and solvents enter the aromatic stripping column from the bottom of the de-aromatization column, and rich aromatic components are obtained from the bottom of the aromatic stripping column; the solvents separated from the tops of the alkane stripping column and the aromatic stripping column enter the solvent recovery column, and the recovered solvents are respectively recycled to the extraction column and the de-aromatization column from the top of the solvent recovery column.

[0073] Among them, the solvent used is pentane. The pressure of the extraction column is controlled at 4.0 Mpa, the pressure of the de-aromatization column is controlled at 4.2 Mpa, the pressure of the alkane stripping column is controlled at 0.75 Mpa, the pressure of the aromatic stripping column is 0.75 MPa, and the pressure of the solvent recovery column is 4.2 Mpa.

[0074] (3) Mix the high-solid slurry and the deoiled asphalt in the feed mixer and then enter the asphalt stripping column. Control the pressure of the asphalt stripping column at 1.0 MPa and the temperature at 220 °C. The penetration of the asphalt product obtained after removing the solvent is 23 dmm, and the softening point is 58 °C, meeting the requirements of the AH-30 heavy traffic road asphalt product;

[0075] (4) Filter the rich aromatic components obtained at the bottom of the de-aromatization column successively through an oil product filter to remove the impurities introduced in the heavy oil, and then remove the fine particles and impurity sulfur contained through hydrotreating in a hydrofining reactor to obtain a rich aromatic oil product with a solid content of 17 ppm and a sulfur content of 0.460%.

[0076] Comparative Example 1

[0077] This comparative example provides a blended asphalt, and the formula of the blended asphalt is as follows:

[0078] 54.0 g of FCC slurry; 72.0 g of vacuum residue; 74.0 g of deoiled asphalt (DOA), and 6.0 g of ethylene-tetrafluoroethylene copolymer (ETFE).

[0079] The specific preparation method of the ETFE-modified FCC slurry blended asphalt comprises the following steps:

[0080] S1: Mix FCC slurry, vacuum residue, and deoiled asphalt (DOA) according to the above masses to obtain a first mixture;

[0081] S2: Heat the first mixture to a flowing state, then add the formulated amount of ethylene-tetrafluoroethylene copolymer, and mechanically stir at 170 °C for 30 min until fully mixed. Then continue to perform high-speed shearing at a speed of 13,000 rpm for 30 min to obtain 206.0 g of ETFE-modified FCC slurry blended asphalt.

[0082] The asphalt product prepared in this comparative example ensures the performance of the blended asphalt by introducing a polymer. Although it does not meet the AH-70 standard, it is close to the AH-70 standard, and the additionally introduced polymer will also increase the preparation cost of the asphalt product; in addition, this scheme does not efficiently utilize the slurry.

[0083] Comparative Example 2

[0084] This comparative example provides a blended asphalt, and the formula of this blended asphalt is as follows:

[0085] A mixture of Changqing Petrochemical deasphalted asphalt (penetration at 25 °C is 5 - 10 dmm, softening point is 50 - 85 °C), light asphalt (penetration at 25 °C is 200 - 300 dmm), surfactant alkyl phenyl sulfonate, and liquid rosin is mixed and stirred evenly at a temperature of 130 °C and a stirring speed of 500 r / min according to a mass ratio of 10:20:1. Samples are taken every 10 min to detect the viscosity. When the difference between two consecutive detections does not exceed 20 mPa·s, the blended liquid asphalt is obtained.

[0086] The asphalt liquid obtained after blending meets the petroleum asphalt quality standard of IVB / SHT0522 - 2010, meets the requirements of the Highway Engineering Asphalt and Asphalt Mixture Test Procedures (JTG E20 - 2011, the industry standard of the People's Republic of China), meets the index requirements specified in GB No. 200 asphalt, meets the use standards for prime coat oil, tack coat oil, and seal coat oil in road paving, meets the requirements for the preparation raw materials of road asphalt pavement functional repair agents, and meets the standards for special asphalt used for highway maintenance micro-surfacing.

[0087] However, this blended liquid asphalt does not meet the standard of heavy traffic road petroleum asphalt in GB / T 15180 - 2010.

[0088] Of course, the present invention may have many other embodiments. Without departing from the spirit and essence of the present invention, those skilled in the art can make various corresponding changes and modifications according to the present invention. However, these corresponding changes and modifications should fall within the protection scope of the claims of the present invention.

Claims

1. A preparation method of heavy traffic road asphalt, characterized in that, it comprises the following steps: (1) The catalytic cracking slurry passes through the slurry de-solidification unit to obtain clarified slurry and high-solid slurry; (2) The clarified slurry and heavy oil are separated in the solvent deasphalting unit to obtain an alkane-rich component, an aromatic-rich component and deoiled asphalt; (3) After the high-solid slurry and the deoiled asphalt are stripped of the solvent in the asphalt stripping unit, heavy traffic road asphalt is obtained.

2. The preparation method of heavy traffic road asphalt according to claim 1, characterized in that, The density of the catalytic cracking slurry is 0.95 to 1.1 g / cm 3 , the ash content is 0.020% to 0.110%, and the solid content is 2,000 to 7,000 ppm.

3. The preparation method of heavy traffic road asphalt according to claim 1, characterized in that, the solid content of the clarified slurry is 0-200 ppm.

4. The preparation method of heavy traffic road asphalt according to claim 1, characterized in that, the slurry de-solidification unit includes a filtration buffer tank, a high-temperature slurry pump and a membrane filter connected in sequence, and the membrane filter includes 1 group of metal membranes or 2-3 groups of metal membranes connected in series; the filtration temperature of the membrane filter is 70-200 °C.

5. The preparation method of heavy traffic road asphalt according to claim 1, characterized in that, the heavy oil is selected from at least one of vacuum residue of naphthenic crude oil, vacuum residue of intermediate crude oil and oil sand asphalt; and / or the mass ratio of the clarified slurry to the heavy oil is 1:1-20.

6. The preparation method of heavy traffic road asphalt according to claim 1, characterized in that, the solvent deasphalting unit includes an extraction column, a dearomatization column, an alkane stripping column, an aromatic stripping column and a solvent recovery column, and the clarified slurry buffer tank and the heavy oil buffer tank are respectively connected to the extraction column through a clarified slurry and heavy oil mixer.

7. The preparation method of heavy traffic road asphalt according to claim 6, characterized in that, the alkane-rich component, the aromatic-rich component and the deoiled asphalt are respectively obtained at the bottoms of the alkane stripping column, the aromatic stripping column and the extraction column; preferably, the pressures of the extraction column, the dearomatization column and the solvent recovery column are 4.0-5.0 MPa, and the pressures of the alkane stripping column and the aromatic stripping column are 0.5-1.0 MPa.

8. The preparation method of heavy traffic road asphalt according to claim 6, characterized in that, the solvents used in the extraction column and the dearomatization column in the solvent deasphalting unit are selected from alkanes of C3-C5, preferably at least one of propane, n-butane, pentane and isobutane.

9. The preparation method of heavy traffic road asphalt according to claim 6, characterized in that, the asphalt stripping unit includes a feed mixer and an asphalt stripping column; the high-solid slurry and the deoiled asphalt obtained at the bottom of the extraction column are mixed in the feed mixer and then enter the asphalt stripping column for stripping, and the solvent obtained by stripping is recycled to the solvent recovery column, and the heavy traffic road asphalt product is obtained at the bottom of the stripping column; the pressure of the asphalt stripping column is 0.3-1.2 Mpa, and the temperature is 110-250 °C.

10. The preparation method of heavy traffic road asphalt according to claim 1, characterized in that, It further includes the step of sending the aromatic-rich component into a deep purification unit for deep purification to obtain purified aromatic-rich oil, and the deep purification unit includes an oil filter and a hydrofining reactor connected in sequence; The solid content of the purified aromatic-rich oil is 0 to 20 ppm, and the sulfur content is less than 0.5%.

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