A road petroleum pitch and a method for producing the same

Abstract

The application discloses a road petroleum asphalt and a preparation method thereof. The road petroleum asphalt comprises the following components in parts by weight: a pretreatment component: 100 parts; modified residue reduction: 10-80 parts; wherein the modified residue reduction comprises the following components in parts by weight: inferior residue reduction: 100 parts; a modifier: 0.5-6 parts. The inferior residue reduction is used as raw material, and an asphalt product meeting the requirements of BND 60 / 90 of Kazakhstan road asphalt is obtained.

Description

Technical Field

[0001] This invention relates to a petroleum asphalt and its preparation method, and particularly to a road petroleum asphalt and its preparation method. Background Technology

[0002] As crude oil becomes increasingly heavy, the yield of vacuum residue is gradually increasing, leading to higher levels of heavy metals and sulfur in the residue. This makes the processing of the residue into lighter forms more difficult. However, using inferior vacuum residue to produce asphalt is a relatively simple and economically efficient processing method. China's asphalt production mainly employs a distillation and blending process. But with the deterioration of vacuum residue quality, the relative content of saturated components and asphaltenes increases, while the relative content of aromatics and resins decreases. Furthermore, the asphaltenes exhibit increased association and more complex forms. Under these circumstances, it is difficult to produce qualified road asphalt using a simple distillation and blending process.

[0003] For example, Tarim River heavy oil is an important petroleum resource, but its structure, composition, and physicochemical properties differ greatly from other oil sources. Tarim River vacuum residue yields over 70%, and it is characterized by high sulfur, high residual carbon, high asphaltenes, and high heavy metal content. When this type of inferior crude oil is used to prepare asphalt, it often results in a low flash point, making it difficult to meet the flash point requirements of the "Technical Specifications for Highway Asphalt Construction" (JTG F40-2004) for "Technical Requirements for Road Petroleum Asphalt."

[0004] In some cold-climate countries, such as Russia and Kazakhstan, there are strict requirements for the low-temperature performance of asphalt. Kazakhstan's national road asphalt standard (CTPK 1373-2005) uses penetration at 0°C, elongation at 0°C, and brittle point as indices to limit the low-temperature performance of asphalt. For example, the Kazakhstani road asphalt standard requires that the brittle point of 60 / 90 and 90 / 130 grades not exceed -18°C and -20°C, respectively. Similarly, in Russia's oil road asphalt standard (гост33133-2014), the brittle point of 70 / 100 and 100 / 130 grades of asphalt is required to be no greater than -18°C and -20°C before the thin-film oven test, and also no greater than -15°C and -17°C after the test. However, these countries do not have high requirements for the flash point of asphalt.

[0005] If the Tarim River heavy oil, a raw material unsuitable for producing Grade A road asphalt, could be used in Xinjiang, China, to produce the aforementioned road asphalt, it would reduce the difficulty of utilizing inferior heavy oil and increase the added value of such raw materials.

[0006] CN110872446A discloses a modified road asphalt and its preparation method. This modified road asphalt meets the relevant requirements of Kazakhstan's BND 60 / 90 standard for road asphalt. However, this method does not achieve high-value-added utilization of inferior resources and is not economically viable.

[0007] In summary, the methods described above are unsuitable for producing Kazakhstani standard road asphalt from inferior raw materials. Therefore, for raw materials with high asphalt content and low aromaticity, it is necessary to develop new asphalt production processes to increase the added value of low-quality resources. Summary of the Invention

[0008] To address the shortcomings of existing technologies, this invention provides a road petroleum asphalt and its preparation method. Using difficult-to-process, low-quality slag as raw material, this invention yields an asphalt product that meets the BND 60 / 90 requirements for road asphalt in Kazakhstan.

[0009] This invention provides a road petroleum asphalt, comprising, by weight, the following raw material components: pretreatment component: 100 parts; modified slag-reducing agent: 10-80 parts, preferably 20-50 parts; wherein the modified slag-reducing agent, by weight, comprises the following raw material components:

[0010] Inferior slag reduction: 100 portions;

[0011] Modifier: 0.5-6 parts, preferably 1-5 parts;

[0012] The modifier is one or more of the following: zinc hydroxystannate, hydroquinone, zinc dimethyl thiocarbamate, zinc stearate, urea, thiourea, thiocarbamate, disodium thiodipropionate, disodium thiodipropionate, di(tridecyl) thiodipropionate, and distearate thiodipropionate.

[0013] The modifier is preferably at least two of zinc hydroxystannate, hydroquinone, zinc dimethyl thioaminoformate, and dodecyl thiodipropionate.

[0014] The pretreatment components, by weight, include the following raw material components:

[0015] Inferior slag reduction: 100 portions;

[0016] Medium-quality component: 20-60 parts, preferably 25-50 parts;

[0017] Lightweight component: 5-35 parts, preferably 10-30 parts.

[0018] The inferior slag in the pretreatment component and the inferior slag in the anhydride treatment component only need to meet the following properties, and the properties of the two can be exactly the same or different.

[0019] The properties of the inferior slag include: a flash point of 241–256℃, a sulfur content of 2.61 wt%–3.65 wt%, and by mass fraction, saturated components of 26.1%–37.7%, aromatic components of 20.2%–34.5%, resins of 18.3%–24.8%, and asphaltenes of 21.3%–30.1%, with asphaltenes preferably being 21.3%–26.0%.

[0020] The inferior slag also has the following properties: residual carbon value of 21wt% to 29wt%, nitrogen content of 0.14wt% to 0.61wt%, total nickel and vanadium content of 320 to 365μg / g, and condensation index CI of 0.26 to 0.35.

[0021] The inferior reduced slag can be Tarim River reduced slag or other reduced slag that meets the above properties, and the inferior reduced slag is a fraction with an initial boiling point greater than 425°C.

[0022] The intermediate component refers to the resin obtained after solvent deasphalting, and the intermediate component has the following properties: kinematic viscosity of 50 mmHg at 100°C. 2 / s~65mm 2 / s, flash point is 206℃~220℃, by mass fraction, saturated fraction accounts for 30%~42%, aromatic fraction accounts for 48%~57%, resin accounts for 8%~13%, asphaltene content is less than 2%; weight average molecular weight is 1990~2140, molecular weight distribution width is 1.6~3.7.

[0023] The light component refers to vacuum-pressed wax oil, which has the following properties: kinematic viscosity at 50°C is 10 mmHg. 2 / s~16mm 2 / s, density at 20℃ is 760~900kg / m³ 3 By mass fraction, the saturated fraction accounts for 60%–78%, the aromatic fraction accounts for 20%–32%, and the total content of resins and asphaltenes is less than 6%; the residual carbon is less than 0.15%, the sulfur content is less than 0.3%, the nitrogen content is less than 1%, and the hydrogen-to-carbon ratio is 1.5–1.8.

[0024] This invention also provides a method for preparing road petroleum asphalt, which includes the following steps:

[0025] (1) Preparation of modified slag-reducing agent;

[0026] (2) Preparation of pretreatment components;

[0027] (3) The materials obtained in step (1) and step (2) are mixed and statically heated to finally obtain road petroleum asphalt.

[0028] The preparation process of the modified slag-reducing agent is as follows:

[0029] a. Add the inferior slag heated to a fluid state into the reactor, keep oxidizing gas flowing through it and heat it to a specific temperature, then continue stirring to carry out oxidation treatment;

[0030] b. Add the modifier to the material obtained in step a, introduce protective gas, stir evenly, heat to the reaction temperature, carry out condensation reaction, and obtain modified slag after the reaction is completed.

[0031] In step a, the reactor is a high-pressure reactor, and the initial temperature of the reactor is adjusted to 120-130℃.

[0032] In step a, the heating to the reaction temperature is performed using a programmed temperature rise method, with a heating rate of 1–3 °C / min, and the reaction temperature is 150 °C–200 °C, preferably 150 °C–170 °C. The reaction time is 60–120 min. The stirring speed is 600–800 r / min.

[0033] In step a, the oxidizing gas is oxygen-enriched air (oxygen volume content of 30%–55%), and the gas flow rate is 0.06–0.4 m³ / s. 3 / kg / h.

[0034] In step b, the protective gas is an inert gas and / or N2, and the gas flow rate is 0.05–0.25 m³ / h. 3 / kg / h, the condensation reaction time is 20-80 min, the stirring speed during condensation is 100-240 r / min, and the condensation temperature is 180℃-200℃.

[0035] The preparation process of the pretreatment component is as follows:

[0036] i. After heating the inferior slag to a fluid state, mix it with the medium and light components, and then perform hydrogenation treatment together with hydrogen.

[0037] ii. Perform atmospheric and vacuum distillation on the material obtained in step i to obtain the final pretreated components.

[0038] In step i, the operating conditions for the hydrogenation treatment are: reaction temperature of 365℃~390℃, reaction pressure of 12MPa~22MPa, and volume hourly space velocity of 0.5~1.8h. -1 The hydrogen-to-oil volume ratio is 400–1500; the preferred operating conditions are: reaction temperature 370–390℃, reaction pressure 13–20 MPa, and volume hourly space velocity (VHSV) 0.5–1.2 h⁻¹. -1 The hydrogen-to-oil volume ratio is 500–1100.

[0039] In step i, the reactor used for the hydrogenation treatment can be a fixed-bed hydrogenation reactor, a fluidized-bed hydrogenation reactor, or a suspended-bed hydrogenation reactor, with a fluidized-bed hydrogenation reactor being preferred.

[0040] In step i, the catalyst used for the hydrogenation treatment can be a commercially available catalyst, such as the FF, FH, and FZC series catalysts developed by the Dalian Research Institute of Petrochemical Technology, Sinopec. The catalyst gradation method can be determined according to conventional methods, and is not particularly limited in this invention.

[0041] In step ii, the atmospheric and vacuum distillation is carried out in an atmospheric and vacuum distillation kettle. Atmospheric distillation has no special requirements. The final temperature of vacuum distillation is 465–540°C, preferably 485–520°C.

[0042] In step (3), the stirring speed of the blending process is 700-900 r / min, the stirring time is 4-6 h, and the blending temperature is 140℃-165℃.

[0043] In step (3), the static heat preservation treatment needs to be carried out under inert gas and / or N2, maintaining the temperature at 135℃~150℃, and the heat preservation time is 6~10h.

[0044] Compared with the prior art, the road petroleum asphalt and its preparation method of the present invention have the following advantages:

[0045] (1) This invention uses inferior asphalt residue as raw material, which is unsuitable for producing Grade A road asphalt or Kazakhstani road asphalt. For example, Tarim asphalt residue has a high asphalt content, a very special form, and extremely poor overall performance. This invention uses inferior asphalt residue in combination with a modifier. After oxidation, condensation, and other treatments, modified asphalt residue can be obtained. This modified asphalt residue is then combined with pretreated components to obtain road petroleum asphalt with excellent comprehensive performance. All properties can meet the technical requirements of the corresponding grade of "Kazakhstani Road Asphalt" (CTPK 1373-2005).

[0046] (2) The present invention also introduces a pretreatment component, which is obtained by hydrogenation treatment and secondary distillation of inferior slag, medium component and light component. The treatment process adjusts and optimizes the average molecular structure and molecular weight distribution of the material, and enhances the continuity of the material structure and composition. This pretreatment component has the characteristics of low viscosity, high flash point, large low temperature ductility and low temperature sensitivity, which can make up for the defects of inferior slag.

[0047] (3) The pretreatment components introduced in this invention are well compatible with modified slag reduction. After blending, they can take into account the high and low temperature performance of asphalt. The colloidal structure can be optimized without mixing and distillation, thereby improving the comprehensive indicators of asphalt. Furthermore, it has good low temperature elongation, eliminating the step of polymer mild modification and extension. The resulting road petroleum asphalt has the characteristics of low brittleness and excellent anti-aging performance. Detailed Implementation

[0048] The technical solution of the present invention is further described below through embodiments, but these embodiments cannot limit the scope of protection of the present invention, and the wt% involved refers to the mass fraction.

[0049] Example 1

[0050] (1) 100 parts of Tahe slag heated to a fluid state (some properties are shown in Table 1) were added to a high-pressure reactor at 120℃ and stirred. Oxygen-enriched air (oxygen volume content of 45%) was introduced at a flow rate of 0.15 m³ / min. 3 Oxidation was carried out at a stirring speed of 700 r / min and a temperature increase of 2 °C / min to 150 °C for 60 min. After oxidation, the temperature was increased to 180 °C and 1 part hydroquinone and 2 parts disodium thiodipropionate were added. N2 was then introduced to induce condensation at a gas flow rate of 0.18 m³ / h. 3 / kg / h, condensation time of 30min, stirring speed of 200r / min, thus obtaining the modified slag-reducing agent.

[0051] (2) 100 parts of Tahe slag heated to a fluid state (properties same as in step (1)), 35 parts of medium-quality components (some properties are shown in Table 2), and 20 parts of light-quality components (some properties are shown in Table 3) were reacted at a reaction temperature of 380℃, a reaction pressure of 16MPa, and a volume hourly space velocity of 0.8h. -1 Hydrogenation was carried out under a hydrogen-to-oil volume ratio of 900. The hydrogenation catalyst was the FZC series catalyst developed by the Dalian Petrochemical Research Institute of Sinopec. The hydrogenation product was then subjected to atmospheric and vacuum distillation. The product distilled at temperatures above 500°C was the required pretreatment component.

[0052] (3) 30 parts of the modified slag reduction obtained in (1) and 100 parts of the pretreatment component obtained in (2) were blended. The stirring speed during blending was 750 r / min, the temperature was 155℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt A1.

[0053] Example 2

[0054] (1) 100 parts of Tahe slag heated to a fluid state (some properties are shown in Table 1) were added to a high-pressure reactor at 120℃ and stirred. Oxygen-enriched air (oxygen volume content of 45%) was introduced at a flow rate of 0.15 m³ / min. 3 The solution was prepared at a rate of / kg / h, stirred at 700 rpm, and heated to 160°C at a rate of 2°C / min for 60 min. After oxidation, the temperature was raised to 185°C, and 1 part zinc hydroxystannate and 2 parts zinc dimethyl thiocarbamate were added. N2 was then introduced to induce condensation at a gas flow rate of 0.21 m³ / h. 3 / kg / h, condensation time of 30min, stirring speed of 200r / min, thus obtaining the modified slag-reducing agent.

[0055] (2) 100 parts of Tahe slag heated to a fluid state (properties same as in step (1)), 30 parts of medium-quality components (some properties are shown in Table 2), and 25 parts of light-quality components (some properties are shown in Table 3) were reacted at a reaction temperature of 380℃, a reaction pressure of 16MPa, and a volume hourly space velocity of 0.8h. -1 Hydrogenation was carried out under a hydrogen-to-oil volume ratio of 900. The hydrogenation catalyst was the FZC series catalyst developed by the Dalian Petrochemical Research Institute of Sinopec. The hydrogenation product was distilled under atmospheric and vacuum conditions. The product distilled at a temperature greater than 495℃ was the required pretreatment component.

[0056] (3) 25 parts of the modified slag reduction obtained in (1) and 100 parts of the pretreatment component obtained in (2) were blended. The stirring speed during blending was 750 r / min, the temperature was 150℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt A2.

[0057] Example 3

[0058] (1) 100 parts of Tahe slag heated to a fluid state (some properties are shown in Table 1) were added to a high-pressure reactor at 120℃ and stirred. Oxygen-enriched air (oxygen volume content of 50%) was introduced at a flow rate of 0.12 m³ / min. 3 The solution was prepared at a rate of / kg / h, stirred at 720r / min, and heated to 160℃ at a rate of 2℃ / min for 60min. After oxidation, the temperature was raised to 185℃ and 2 parts hydroquinone and 2 parts zinc dimethyl thiocarbamate were added. N2 was then introduced to induce condensation at a gas flow rate of 0.20m³ / h. 3 / kg / h, condensation time of 40min, stirring speed of 200r / min, thus obtaining the modified slag-reducing agent.

[0059] (2) 100 parts of Tahe slag heated to a fluid state (properties same as in step (1)), 30 parts of medium-quality components (some properties are shown in Table 2), and 25 parts of light-quality components (some properties are shown in Table 3) were reacted at a reaction temperature of 380℃, a reaction pressure of 16MPa, and a volume hourly space velocity of 0.8h. -1 Hydrogenation was carried out under a hydrogen-to-oil volume ratio of 900. The hydrogenation catalyst was the FZC series catalyst developed by the Dalian Petrochemical Research Institute of Sinopec. The hydrogenation product was distilled under atmospheric and vacuum conditions. The product distilled at a temperature greater than 490℃ was the required pretreatment component.

[0060] (3) 25 parts of the modified slag reduction obtained in (1) and 100 parts of the pretreatment component obtained in (2) were blended. The stirring speed during blending was 750 r / min, the temperature was 150℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt A3.

[0061] Example 4

[0062] (1) 100 parts of Tahe slag heated to a fluid state (some properties are shown in Table 1) were added to a high-pressure reactor at 120℃ and stirred. Oxygen-enriched air (oxygen volume content of 45%) was introduced at a flow rate of 0.21 m³ / min. 3 The solution was prepared at a rate of / kg / h, stirred at 720r / min, and heated to 160℃ at a rate of 2℃ / min for 80min. After oxidation, the temperature was raised to 185℃ and 1 part zinc hydroxystannate and 2 parts zinc dimethylthiocarbamate were added. N2 was then introduced to induce condensation at a gas flow rate of 0.21m³. 3 / kg / h, condensation time of 55min, stirring speed of 240r / min, thus obtaining the modified slag-reducing agent.

[0063] (2) 100 parts of Tahe slag heated to a fluid state (properties same as in step (1)), 35 parts of medium-quality components (some properties are shown in Table 2), and 25 parts of light-quality components (some properties are shown in Table 3) were reacted at a reaction temperature of 380℃, a reaction pressure of 16MPa, and a volume hourly space velocity of 0.8h. -1 Hydrogenation was carried out under a hydrogen-to-oil volume ratio of 900. The hydrogenation catalyst was the FZC series catalyst developed by the Dalian Petrochemical Research Institute of Sinopec. The hydrogenation product was then subjected to atmospheric and vacuum distillation. The product distilled at temperatures above 500°C was the required pretreatment component.

[0064] (3) 20 parts of the modified slag reduction obtained in (1) and 100 parts of the pretreatment component obtained in (2) were blended. The stirring speed during blending was 750 r / min, the temperature was 150℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt A4.

[0065] Comparative Example 1

[0066] (1) Prepare the modified slag reducing agent according to Example 1.

[0067] (2) 100 parts of Tahe slag heated to a fluid state, 35 parts of medium components (some properties are shown in Table 2), and 20 parts of light components were directly mixed to obtain a mixture.

[0068] (3) 30 parts of the modified slag reduction material obtained in (1) and 100 parts of the mixture obtained in (2) were blended. The stirring speed was 750 r / min, the temperature was 155℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt B1.

[0069] Comparative Example 2

[0070] Same as Example 1, except that the slag reduction process is not performed in step (1), and B2 is finally obtained. Specifically:

[0071] (1) 100 parts of Tahe slag heated to a fluid state (properties same as in Example 1), 35 parts of medium-weight components (some properties are shown in Table 2), and 20 parts of light-weight components (some properties are shown in Table 3) were reacted at a reaction temperature of 380°C, a reaction pressure of 16 MPa, and a volume hourly space velocity of 0.8 h⁻¹. -1 Hydrogenation was carried out under a hydrogen-to-oil volume ratio of 900. The hydrogenation catalyst was the FZC series catalyst developed by the Dalian Petrochemical Research Institute of Sinopec. The hydrogenation product was then subjected to atmospheric and vacuum distillation. The product distilled at temperatures above 500°C was the required pretreatment component.

[0072] (3) 30 parts of Tahe slag reduction were blended with 100 parts of the pretreatment components obtained in (1). The stirring speed was 750 r / min, the temperature was 155℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt B2.

[0073] Comparative Example 3

[0074] Same as Example 1, except that no modifier is added during the slag reduction process in step (1), and B3 is finally obtained. Specifically:

[0075] (1) 100 parts of Tahe slag heated to a fluid state (some properties are shown in Table 1) were added to a high-pressure reactor at 120℃ and stirred. Oxygen-enriched air (oxygen volume content of 45%) was introduced at a flow rate of 0.15 m³ / min. 3 / kg / h, under a stirring speed of 700r / min, and with the temperature increased to 150℃ at a rate of 2℃ / min for oxidation, and the oxidation time was 60min, the modified slag-reducing agent was obtained.

[0076] (2) 100 parts of Tahe slag heated to a fluid state (properties same as in step (1)), 35 parts of medium-quality components (some properties are shown in Table 2), and 20 parts of light-quality components (some properties are shown in Table 3) were reacted at a reaction temperature of 380℃, a reaction pressure of 16MPa, and a volume hourly space velocity of 0.8h. -1 Hydrogenation was carried out under a hydrogen-to-oil volume ratio of 900. The hydrogenation catalyst was the FZC series catalyst developed by the Dalian Petrochemical Research Institute of Sinopec. The hydrogenation product was then subjected to atmospheric and vacuum distillation. The product distilled at temperatures above 500°C was the required pretreatment component.

[0077] (3) 30 parts of the modified slag reduction obtained in (1) and 100 parts of the pretreatment component obtained in (2) were blended. The stirring speed during blending was 750 r / min, the temperature was 155℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt B3.

[0078] Comparative Example 4

[0079] Same as Example 1, except that no pretreatment components are introduced during the preparation process, ultimately yielding B4. Specifically:

[0080] (1) 100 parts of Tahe slag heated to a fluid state (some properties are shown in Table 1) were added to a high-pressure reactor at 120℃ and stirred. Oxygen-enriched air (oxygen volume content of 45%) was introduced at a flow rate of 0.15 m³ / min. 3 Oxidation was carried out at a stirring speed of 700 r / min and a temperature increase of 2 °C / min to 150 °C for 60 min. After oxidation, the temperature was increased to 180 °C and 1 part hydroquinone and 2 parts disodium thiodipropionate were added. N2 was then introduced to induce condensation at a gas flow rate of 0.18 m³ / h. 3 / kg / h, condensation time of 30min, stirring speed of 200r / min, thus obtaining the modified slag-reducing agent.

[0081] (2) 30 portions of the modified slag-reducing material obtained in (1) were blended and treated. The stirring speed was 750 r / min, the temperature was 155℃, and the stirring time was 6 h. After the stirring was completed, the mixture was statically kept at 145℃ under N2 atmosphere for 8 h to obtain the final road petroleum asphalt B4.

[0082] Test case

[0083] Key index tests were conducted on the Tarim Basin asphalt, medium-grade component, light-grade component, and road petroleum asphalt obtained from the examples and comparative examples (in accordance with the Test Procedure for Asphalt and Asphalt Mixtures for Highway Engineering JTG E20-2011), and the results were compared with the corresponding grade technical indexes of "Kazakhstan Road Asphalt" (CTPK 1373-2005).

[0084] Table 1. Properties of the Tarim Basin Slag Reduction Section Used in Examples and Comparative Examples

[0085]

[0086]

[0087] Table 2. Partial properties of the medium-sized components used in the examples and comparative examples.

[0088] Saturated fraction / wt% 32.37 Aromatic components / wt% 56.15 Gel / wt% 11.41 Asphalt content wt / % 0.07 <![CDATA[Kinematic viscosity at 100 °C / mm 2 / s]]> 53 Flash point / °C 213 weight average molecular weight 2135 Molecular weight distribution width 2.2

[0089] Table 3. Partial Properties of Lightweight Components Used in Examples and Comparative Examples

[0090]

[0091]

[0092] Table 4. Main properties of the examples and comparative examples

[0093]

[0094] Continued from Table 4

[0095]

[0096] The scope of protection of this invention is not limited to the above embodiments, but is defined by the claims. Those skilled in the art can make appropriate modifications to these embodiments without departing from the technical concept and spirit of this invention, and these modified embodiments are also included within the scope of protection of this invention.

Claims

1. A type of road petroleum asphalt, comprising the following raw material components by weight: pretreatment component: 100 parts; modified slag-reducing component: 10-80 parts; The modified slag-reducing agent, by weight, includes the following raw material components: Inferior slag reduction: 100 portions; Modifier: 0.5~6 parts; The modifier is at least two of zinc hydroxystannate, hydroquinone, zinc dimethyl thiocarbamate, and dodecyl thiodipropionate. The pretreatment components, by weight, include the following raw material components: Inferior slag reduction: 100 portions; Medium-quality components: 20-60 parts; Light components: 5-35 parts; The properties of the inferior reduced-pressure residue include: a flash point of 241~256℃, a sulfur content of 2.61wt%~3.65wt%, and by mass fraction, a saturated fraction of 26.1%~37.7%, an aromatic fraction of 20.2%~34.5%, a resinous fraction of 18.3%~24.8%, an asphaltenes fraction of 21.3%~30.1%, a carbon residue of 21wt%~29wt%, a nitrogen content of 0.14wt%~0.61wt%, a total nickel and vanadium content of 320~365μg / g, and a condensation index CI of 0.26~0.35; the inferior reduced-pressure residue is a fraction with an initial boiling point greater than 425℃. The intermediate component refers to the resin obtained after solvent deasphalting, and the intermediate component has the following properties: kinematic viscosity of 50 mmHg at 100°C. 2 / s~65mm 2 / s, flash point is 206℃~220℃, by mass fraction, saturated fraction accounts for 30%~42%, aromatic fraction accounts for 48%~57%, resin accounts for 8%~13%, asphaltene content is less than 2%; weight average molecular weight is 1990~2140, molecular weight distribution width is 1.6~3.7; The light component refers to vacuum-pressed wax oil, which has the following properties: kinematic viscosity at 50°C is 10 mmHg. 2 / s~16mm 2 / s, density at 20℃ is 760~900 kg / m³ 3 By mass fraction, the saturated fraction accounts for 60%~78%, the aromatic fraction accounts for 20%~32%, the total content of resins and asphaltenes is less than 6%; the residual carbon is less than 0.15%, the sulfur content is less than 0.3%, the nitrogen content is less than 1%, and the hydrogen-to-carbon ratio is 1.5~1.

8. The preparation process of the pretreatment component is as follows: i. After heating the inferior slag to a fluid state, mix it with the medium and light components, and then perform hydrogenation treatment together with hydrogen. ii. The material obtained in step i is subjected to atmospheric and vacuum distillation to obtain the final pretreated components; The preparation process of the modified slag-reducing agent is as follows: a. Add the inferior slag heated to a fluid state into the reactor, keep oxidizing gas flowing through it and heat it to a specific temperature, then continue stirring to carry out oxidation treatment; b. Add the modifier to the material obtained in step a, introduce protective gas, stir evenly, heat to the reaction temperature, carry out condensation reaction, and obtain modified slag after the reaction is completed.

2. The road petroleum asphalt according to claim 1, characterized in that, The road petroleum asphalt, by weight, comprises the following raw material components: pretreatment component: 100 parts; modified slag-reducing component: 20-50 parts; The modified slag-reducing agent, by weight, includes the following raw material components: Inferior slag reduction: 100 portions; Modifier: 1-5 parts.

3. The road petroleum asphalt according to claim 1, characterized in that, The pretreatment components, by weight, include the following raw material components: Inferior slag reduction: 100 portions; Medium-quality components: 25-50 parts; Lightweight component: 10-30 parts.

4. The method for preparing road petroleum asphalt according to any one of claims 1-3, characterized in that, Includes the following steps: (1) Preparation of modified slag-reducing agent; (2) Preparation of pretreatment components; (3) The materials obtained in step (1) and step (2) are mixed and subjected to static heat preservation treatment to finally obtain road petroleum asphalt; The preparation process of the modified slag-reducing agent is as follows: a. Add the inferior slag heated to a fluid state into the reactor, keep oxidizing gas flowing through it and heat it to a specific temperature, then continue stirring to carry out oxidation treatment; b. Add modifier to the material obtained in step a, introduce protective gas, stir evenly, heat to the reaction temperature, carry out condensation reaction, and obtain modified slag after the reaction is completed; The preparation process of the pretreatment component is as follows: i. After heating the inferior slag to a fluid state, mix it with the medium and light components, and then perform hydrogenation treatment together with hydrogen. ii. Perform atmospheric and vacuum distillation on the material obtained in step i to obtain the final pretreated components.

5. The preparation method according to claim 4, characterized in that, In step a, the heating to the reaction temperature is performed by programmed heating at a rate of 1-3°C / min, the reaction temperature is 150°C-200°C, and the reaction time is 60-120 min; the stirring speed is 600-800 r / min.

6. The preparation method according to claim 4, characterized in that, In step b, the protective gas is an inert gas and / or N2, and the gas flow rate is 0.05~0.25m³. 3 / kg / h, the condensation reaction time is 20~80min, the stirring speed during condensation is 100~240r / min, and the condensation temperature is 180℃~200℃.

7. The preparation method according to claim 4, characterized in that, In step i, the operating conditions for the hydrogenation treatment are: reaction temperature of 365℃~390℃, reaction pressure of 12MPa~22MPa, and volume hourly space velocity of 0.5~1.8h. -1 The hydrogen-to-oil volume ratio is 400-1500.

8. The preparation method according to claim 4, characterized in that, In step ii, the atmospheric and vacuum distillation is carried out in an atmospheric and vacuum distillation kettle, wherein the final temperature of vacuum distillation is 465~540℃.

9. The preparation method according to claim 4, characterized in that, In step (3), the stirring speed of the blending process is 700~900 r / min, the stirring time is 4~6 h, and the blending temperature is 140℃~165℃.

10. The preparation method according to claim 4, characterized in that, In step (3), the static heat preservation treatment needs to be carried out under inert gas and / or N2, maintaining the temperature at 135℃~150℃, and the heat preservation time is 6~10h.

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