Processing method and system of heavy distillate oil
By dearrangement and thermal cracking of the catalytic raw materials, the problem of high scorching rate during the catalytic molecular reaction process is solved, and the long-term operation of the catalytic molecular reaction device and the diversified utilization of heavy distillate oil are realized.
Patent Information
- Application Number
- CN202311865554.3
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2023-12-29
- Publication Date
- 2025-07-01
AI Technical Summary
In the prior art, the catalytic burn rate during the catalytic molecular reaction is high, resulting in an increase in carbon emissions and is not conducive to the long-term operation of the catalytic molecular reaction device.
After catalytic molecular reaction of the catalytic raw materials, the refining oil is subjected to dearrative treatment, and the first molecular component and second molecular component raw oil with different aromatic content are separated out. The first molecular component raw oil with a low aromatic content is used as the catalytic raw material together with the heavy distillate oil to be processed, and the catalytic molecular reaction treatment is continued. At the same time, the second molecular component raw oil rich in aromatic hydrocarbons is thermally cracked to produce chemical products such as carbon black and needle coke.
It effectively reduces the catalytic burn rate during catalytic molecular reaction, reduces carbon emissions, and realizes the diversified utilization of heavy distillate oil, alleviates the problem of device blockage, and improves the long-term operation capability of device.
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Figure CN120230587A_ABST
Abstract
Description
Technical Field
[0001] The invention relates to the technical field of oil refining, and in particular to a processing method and system for heavy distillate oil. Background Art
[0002] The reaction device of catalytic molecular reaction is the core device used by the refinery to process heavy distillate oil. In the prior art, the gasoline component produced by the catalytic molecular reaction device accounts for a large proportion of the gasoline output of the entire refinery (up to 60% to 80%). In the process of catalytic molecular reaction, recycled oil is one of the reaction products of the catalytic molecular reaction, and its components include aromatics (usually 40% to 70%) and residual carbon (content is about 0.2% to 1.1%). Due to the high content of residual carbon in recycled oil, the recycling burn rate of recycled oil is also high (up to 10% to 20%, or even higher). The high recycling burn rate will greatly increase the catalytic burn rate of the entire catalytic molecular reaction process, increase carbon emissions, and is also not conducive to the long-term operation of the reaction device of the catalytic molecular reaction.
[0003] Therefore, how to effectively reduce the catalytic burning rate during the catalytic molecular reaction process and reduce carbon emissions is a technical problem that needs to be solved urgently. Summary of the invention
[0004] In view of the above problems, the present invention is proposed to provide a method and system for processing heavy distillate oil that overcomes the above problems or at least partially solves the above problems.
[0005] In a first aspect, an embodiment of the present invention provides a method for processing heavy distillate oil, comprising:
[0006] The catalytic raw material is subjected to catalytic molecular reaction treatment to obtain recycled oil and a first chemical product; the catalytic raw material includes: heavy distillate oil to be processed;
[0007] Performing dearomatization on the recycled oil to obtain a first molecular component feedstock oil and a second molecular component feedstock oil; wherein the aromatic content of the first molecular component feedstock oil is less than a first preset threshold, the aromatic content of the second molecular component feedstock oil is greater than a second preset threshold, and the second preset threshold is greater than the first preset threshold;
[0008] The first molecular component raw oil is added into the catalytic raw material, and the catalytic molecular reaction treatment is continued.
[0009] In an optional embodiment, dearomatizing the recycled oil to obtain a first molecular component feedstock oil and a second molecular feedstock oil includes: using a first solvent to extract the recycled oil under preset extraction conditions to obtain the first molecular component feedstock oil and the second molecular feedstock oil.
[0010] In an alternative embodiment, using a first solvent, under preset extraction conditions, the recycled oil is subjected to extraction treatment to obtain a first molecular component feedstock oil and a second molecular component feedstock oil, including:
[0011] Using the first solvent, under preset extraction conditions, the recycled oil is subjected to extraction treatment to obtain the first molecular component feedstock oil and an extraction bottoms;
[0012] The extraction bottoms is subjected to separation treatment to separate out a second grouped component feedstock oil and a second solvent.
[0013] In an alternative embodiment, the preset extraction conditions include: a temperature of 60°C to 100°C and a solvent-to-oil ratio of 2 to 3.
[0014] In an alternative embodiment, the heavy fraction oil processing method provided by the embodiments of the present invention further includes:
[0015] The second molecular component feedstock oil is subjected to thermal cracking treatment to obtain second chemical products; the second chemical products include at least one of carbon black and needle coke.
[0016] In an alternative embodiment, the subjecting the second molecular component feedstock oil to thermal cracking treatment to obtain second chemical products includes:
[0017] Adopting an oil furnace process, under first preset thermal cracking conditions, the second molecular component feedstock oil is subjected to thermal cracking treatment to obtain the carbon black;
[0018] And / or,
[0019] Adopting a coking process, under second preset thermal cracking conditions, the second molecular component feedstock oil is subjected to thermal cracking treatment to obtain the needle coke.
[0020] In an alternative embodiment, the first preset thermal cracking conditions include: a reaction temperature range of 1750°C to 1930°C, the oxygen content of the air participating in the thermal cracking reaction is in the range of 23% - 28%, and the total combustion rate is 26%.
[0021] In an alternative embodiment, the catalytic molecular reaction is a catalytic cracking reaction or a catalytic pyrolysis reaction.
[0022] In an alternative embodiment, the heavy fraction oil processing method provided by the embodiments of the present invention further includes: mixing the catalytic oil slurry included in the first chemical product with a viscosity-reducing liquid in a preset ratio to obtain a first mixture, and filtering the first mixture to remove solids to obtain a second mixture;
[0023] Use the second mixture to provide heat for the extraction treatment of recycled oil, and perform thermal cracking treatment on the second mixture to obtain second chemical products;
[0024] Or,
[0025] Perform dearomatization treatment on the second mixture to obtain a third mixture and a fourth mixture, wherein the aromatic content of the fourth mixture is greater than that of the third mixture;
[0026] Perform thermal cracking treatment on the fourth mixture to obtain second chemical products.
[0027] Based on the same inventive concept, an embodiment of the present invention further provides a processing system for heavy distillate oil, including: a catalytic molecular reaction device and a dearomatization treatment device;
[0028] The catalytic molecular reaction device is used to perform catalytic molecular reaction treatment on a catalytic raw material to obtain recycled oil and first chemical products; the catalytic raw material includes: heavy distillate oil to be processed; and is used to use the first molecular component raw oil obtained from the dearomatization treatment device and the heavy distillate oil to be processed as catalytic raw materials and continue to perform catalytic molecular reaction treatment;
[0029] The dearomatization treatment device is used to perform dearomatization treatment on the recycled oil obtained from the catalytic molecular reaction device to obtain a first molecular component raw oil and a second molecular component raw oil; wherein, the aromatic content of the first molecular component raw oil is less than a first preset threshold, the aromatic content of the second molecular component raw oil is greater than a second preset threshold, and the second preset threshold is greater than the first preset threshold.
[0030] In an optional embodiment, the processing system for heavy distillate oil provided by the embodiment of the present invention further includes: a thermal cracking device;
[0031] The thermal cracking device is used to perform thermal cracking treatment on the second molecular component raw oil obtained from the dearomatization treatment device to obtain second chemical products;
[0032] The second chemical products include at least one of carbon black and needle coke.
[0033] In an optional embodiment, the dearomatization treatment device includes: an extraction tower and a solvent recovery tower;
[0034] The extraction tower is used to use a first solvent to perform extraction treatment on the recycled oil obtained from the catalytic molecular reaction device under preset extraction conditions to obtain the first molecular component raw oil and extraction bottoms;
[0035] The solvent recovery column is used to separate the extraction bottom liquid to obtain the second grouped component feedstock oil and the second solvent.
[0036] The beneficial effects of the above technical solutions provided by the embodiments of the present invention at least include:
[0037] In the processing method of heavy distillate oil provided by the embodiments of the present invention, after catalytic molecular reaction treatment of the catalytic feedstock, the recycled oil obtained is subjected to dearomatization treatment to obtain the first molecular component feedstock oil and the second molecular component feedstock oil; and the first molecular component feedstock oil and the heavy distillate oil to be processed are used together as the catalytic feedstock to continue the catalytic molecular reaction treatment; wherein, the catalytic feedstock includes: the heavy distillate oil to be processed, and the aromatic content of the first molecular component feedstock oil is less than that of the second molecular component feedstock oil; since the first molecular component feedstock oil with a lower aromatic content after dearomatization treatment of the recycled oil is used as the catalytic feedstock together with the heavy distillate oil to be processed, compared with the recycled oil before dearomatization treatment, the carbon residue content of the first molecular component feedstock oil is also correspondingly reduced. Using the first molecular component feedstock oil and the heavy distillate oil to be processed together as the catalytic feedstock for catalytic molecular reaction treatment can effectively reduce the catalytic coking rate in the catalytic molecular reaction process, reduce carbon emissions, and can alleviate the problem that a large amount of coke and other products generated under the condition of a high coking rate block the catalytic molecular reaction device, resulting in the inability of the device to operate in a long cycle.
[0038] At the same time, in the processing method of heavy distillate oil provided by the embodiments of the present invention, the second molecular component feedstock oil rich in aromatic components is subjected to thermal cracking treatment to obtain a second chemical product including at least one of carbon black and needle coke, realizing the diversification of using heavy distillate oil to produce chemical products.
[0039] Other features and advantages of the present invention will be described in the following specification, and, in part, will become apparent from the specification or be understood by implementing the present invention. The objectives and other advantages of the present invention can be achieved and obtained by the structures specifically pointed out in the written specification, claims, and drawings.
[0040] The technical solutions of the present invention will be further described in detail below with reference to the drawings and embodiments. Description of the Drawings
[0041] The drawings are used to provide a further understanding of the present invention, and constitute a part of the specification. They are used together with the embodiments of the present invention to explain the present invention, and do not constitute a limitation to the present invention. In the drawings:
[0042] Figure 1It is a schematic flow chart of the heavy fraction oil processing method in the embodiment of the present invention;
[0043] Figure 2 It is a schematic diagram of the change in the aromatic hydrocarbon content and catalytic coking rate of the first molecular component feedstock oil obtained under the preset extraction conditions and without the preset extraction conditions in the embodiment of the present invention;
[0044] Figure 3 It is a schematic overall flow chart of the heavy fraction oil processing method in the embodiment of the present invention;
[0045] Figure 4 It is a schematic structural diagram of the heavy fraction oil processing system in the embodiment of the present invention. Detailed implementation manners
[0046] Hereinafter, exemplary embodiments of the present disclosure will be described in more detail with reference to the accompanying drawings. Although the exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure can be implemented in various forms and should not be limited by the embodiments set forth herein. On the contrary, these embodiments are provided so that the present disclosure can be more thoroughly understood and the scope of the present disclosure can be fully conveyed to those skilled in the art.
[0047] It should be understood that the "system", "device", "unit" and / or "module" used herein is a method for distinguishing different components, elements, parts, portions or assemblies at different levels. However, if other words can achieve the same purpose, they can be replaced by other expressions.
[0048] As shown in the present application and the claims, unless the context clearly indicates an exception, the words "a", "an", "one" and / or "the" etc. do not specifically refer to the singular and may also include the plural. Generally speaking, the terms "comprising" and "including" only indicate the inclusion of the steps and elements that have been clearly identified, and these steps and elements do not constitute an exclusive list, and the method or device may also include other steps or elements.
[0049] In the present application, flowcharts are used to illustrate the operations performed by the system according to the embodiments of the present application. It should be understood that the operations before or after do not necessarily need to be executed precisely in sequence. On the contrary, the steps can be processed in reverse order or simultaneously. At the same time, other operations can also be added to these processes, or one or several steps can be removed from these processes.
[0050] In order to solve the problem that in the prior art, when using catalytic molecular reaction to process heavy fraction oil, the catalytic coking rate in the catalytic molecular reaction process is relatively high, a processing method and system for heavy fraction oil are proposed.
[0051] The heavy fraction oil processing method provided by the embodiment of the present invention, its flowchart refers toFigure 1 As shown in
[0052] Step S101: Perform catalytic molecular reaction treatment on the catalytic feedstock to obtain recycle oil and the first chemical product; the catalytic feedstock includes: heavy distillate oil to be processed.
[0053] Step S102: Perform dearomatization treatment on the recycle oil to obtain the first molecular component feedstock oil and the second molecular component feedstock oil; wherein, the aromatic hydrocarbon content of the first molecular component feedstock oil is less than the first preset threshold, the aromatic hydrocarbon content of the second molecular component feedstock oil is greater than the second preset threshold, and the second preset threshold is greater than the first preset threshold.
[0054] Step S103: Add the first molecular component feedstock oil to the catalytic feedstock and continue to perform catalytic molecular reaction treatment.
[0055] Among them, during the catalytic molecular reaction process, the catalytic molecular reaction device will separate recycle oil in the fractionating tower. The recycle oil is because not all of the fresh feedstock (such as the heavy distillate oil in this embodiment) can become the required products after one reaction, and there is still a part of the fraction with a distillation range similar to that of the feedstock, which belongs to the intermediate product of the catalytic molecular reaction. The conventional treatment method is to recycle it inside the device, mix it with the fresh feedstock oil and feed it into the riser reactor for catalytic molecular reaction.
[0056] As shown in Table 1, among them, recycle oil 1 is the recycle oil produced by wax oil catalytic cracking, and recycle oils 2 and 3 are the recycle oils produced by two kinds of residue oil catalytic cracking. From the property parameters shown in Table 1, it can be seen that the aromatic hydrocarbon content in the recycle oil produced by residue oil catalytic cracking is relatively high, and the relatively high aromatic hydrocarbon content leads to a relatively high coke burning rate during the catalytic cracking process.
[0057] Table 1
[0058]
[0059]
[0060] The processing method of heavy distillate oil provided by the embodiment of the present invention is as follows: after catalytic molecular reaction treatment of the catalytic raw material, the recycled oil obtained is subjected to dearomatization treatment to obtain a first molecular component feedstock and a second molecular component feedstock; and the first molecular component feedstock and the heavy distillate oil to be processed are used together as the catalytic raw material to continue catalytic molecular reaction treatment; wherein, the catalytic raw material includes: the heavy distillate oil to be processed, and the aromatic hydrocarbon content of the first molecular component feedstock is less than that of the second molecular component feedstock; since the first molecular component feedstock with a lower aromatic hydrocarbon content after dearomatization treatment of the recycled oil is used together with the heavy distillate oil to be processed as the catalytic raw material, compared with the recycled oil before dearomatization treatment, the carbon residue content of the first molecular component feedstock is reduced. Using the first molecular component feedstock and the heavy distillate oil to be processed together as the catalytic raw material for catalytic molecular reaction treatment, compared with the prior art in which the recycled oil and the heavy distillate oil to be processed are used together as the catalytic raw material for catalytic molecular reaction treatment, it can effectively reduce the catalytic coking rate during the catalytic molecular reaction while making full use of the recycled oil, and can reduce carbon emissions during the reaction process.
[0061] Optionally, the aromatic hydrocarbon content referred to above may be the total aromatic hydrocarbon content of the first component feedstock and the second molecular component feedstock. Among them, the first preset threshold may be 25%, and the second preset threshold may be 80%. Preferably, when performing dearomatization treatment, the total aromatic hydrocarbon content of the first molecular component feedstock can be controlled to be as small as possible, and the total aromatic hydrocarbon content of the second molecular component feedstock can be controlled to be as large as possible.
[0062] Optionally, in step S101, the catalytic molecular reaction of the embodiment of the present invention is a catalytic cracking reaction or a catalytic pyrolysis reaction;
[0063] Specifically, in the state where the catalytic molecular reaction is a catalytic cracking reaction, the catalytic raw material can be subjected to catalytic molecular reaction treatment in the following manner to obtain recycled oil and a first chemical product:
[0064] Using a catalytic cracking reaction device, under the first preset reaction conditions, the catalytic raw material is processed to obtain recycled oil and a first chemical product; wherein, the first preset reaction conditions may include: the reaction temperature is 500°C to 520°C.
[0065] In some other embodiments, the catalytic molecular reaction is a catalytic pyrolysis reaction. The catalytic raw material can be subjected to catalytic molecular reaction treatment in the following manner to obtain a first chemical product:
[0066] Using a catalytic pyrolysis reaction device, under the second preset reaction conditions, the catalytic raw material is processed to obtain recycled oil and a first chemical product; wherein, the second preset reaction conditions may include: the reaction temperature is 530°C to 560°C.
[0067] It should be noted that the first preset conditions for catalytic cracking reactions and the second preset conditions for catalytic pyrolysis are only for illustrative purposes. In the actual implementation process, on the premise of ensuring the normal progress of catalytic molecular reactions, the reaction conditions can be appropriately adjusted as needed to reduce the reaction severity (such as the reaction temperature), thereby further reducing the coke burning rate of catalytic molecular reactions and reducing carbon emissions.
[0068] Optionally, in step S102, the recycled oil can be subjected to dearomatization treatment in various ways to obtain the first molecular component feedstock oil and the second molecular feedstock oil. The embodiments of the present invention do not make specific limitations in this regard. Preferably, the recycled oil can be subjected to dearomatization treatment in the following manner: using a first solvent, under preset extraction conditions, the recycled oil is subjected to extraction treatment to obtain the first molecular component feedstock oil and the second molecular feedstock oil.
[0069] Among them, the first solvent may include: one solvent selected from furfural, N-methylpyrrolidone, N,N-dimethylformamide, dimethyl sulfoxide, ethylene glycol methyl ether, or a mixed solvent obtained by mixing multiple solvents;
[0070] The preset extraction conditions include: a temperature of 60°C to 100°C and a solvent-to-oil ratio of 2 to 3.
[0071] Furthermore, using the first solvent, under the preset extraction conditions, the recycled oil is subjected to extraction treatment to obtain the first molecular component feedstock oil and the second molecular component feedstock oil, which may specifically include:
[0072] Using the first solvent, under the preset extraction conditions, the recycled oil is subjected to extraction treatment to obtain the first molecular component feedstock oil and the extraction bottom liquid; among them, the extraction bottom liquid is a mixed liquid of the components remaining in the recycled oil after extracting the first molecular component feedstock oil and the first solvent.
[0073] The extraction bottom liquid is subjected to separation treatment to separate out the second grouped component feedstock oil and the second solvent.
[0074] Among them, both the first solvent and the second solvent are extraction agents used for the extraction treatment of the recycled oil, and the second solvent separated from the extraction bottom liquid can also be added to the first solvent and reused in the dearomatization treatment process of the recycled oil to make full use of the extraction agent and effectively reduce production costs.
[0075] Specifically, the extraction treatment can be carried out in an extraction tower; the separation of the extraction bottom liquid can be carried out in a solvent recovery tower. Through the solvent recovery tower, the solvent components in the extraction bottom liquid can be separated and extracted to obtain the second solvent and the second molecular component feedstock oil.
[0076] It should be noted that during the process of catalytic molecular reaction treatment, the first chemical products generated may also include: dry gas, liquefied gas, gasoline, diesel, etc. And during the catalytic molecular reaction, the single-pass conversion rate of the catalytic molecular reaction can be adjusted according to market needs to reduce the yield of dry gas and the coking rate, and products such as recycle oil, dry gas, liquefied gas, gasoline, diesel, and catalytic slurry can be obtained.
[0077] In an alternative embodiment, for the heavy fraction oil processing method provided by the embodiments of the present invention, after obtaining the second molecular component feedstock oil, it may further include: performing thermal cracking treatment on the second molecular component feedstock oil to obtain second chemical products; the second chemical products include at least one of carbon black and needle coke.
[0078] Since the second molecular component feedstock oil is rich in aromatic components and is a high-quality raw material for thermal cracking reactions, the second molecular component feedstock oil can be processed in various ways to obtain various high-end carbon materials. For example, under oxygen-deficient reaction conditions, the second molecular component feedstock oil can be incompletely burned and pyrolyzed at high temperature to generate chemical products such as carbon black, H2, CO, and CO2.
[0079] Optionally, performing thermal cracking treatment on the second molecular component feedstock oil to obtain second chemical products includes:
[0080] Using the oil furnace process, under the first preset thermal cracking conditions, performing thermal cracking treatment on the second molecular component feedstock oil to obtain carbon black;
[0081] and / or,
[0082] Using the coking process, under the second preset thermal cracking conditions, performing thermal cracking treatment on the second molecular component feedstock oil to obtain needle coke.
[0083] Among them, when using the oil furnace process to produce carbon black, the first preset thermal cracking conditions may include: the reaction temperature range is 1750°C to 1930°C, the oxygen content of the air participating in the thermal cracking reaction is lower than the preset oxygen content threshold, and the total combustion rate (the ratio of the actual air consumption during the reaction to the sum of the air consumption required for the theoretical complete combustion of the fuel and the feedstock oil) is 26%.
[0084] In the specific implementation process, when using the second molecular component feedstock oil to produce carbon black, different properties of carbon black, such as carbon black for rubber, conductive carbon black, pigment carbon black, and other special carbon blacks, can be produced by means of changing the supply amount of process air in the reaction unit, the ratio of process air to fuel and raw materials, and the position of quenching water injection.
[0085] Further, when using the coking process to pyrolyze the second molecular component feedstock under the second preset pyrolysis conditions to obtain the needle coke, the embodiments of the present invention do not specifically limit the second preset pyrolysis conditions, which can be selected according to the prior art as long as the needle coke can be obtained. For example, the second preset pyrolysis conditions may include: the feed temperature range of the coke drum is 450°C to 510°C, the top pressure of the coke drum is 0.6 MPa to 0.9 MPa, and the heating furnace circulation ratio is 0.8 to 1.2.
[0086] Specifically, when using the coking process to pyrolyze the second molecular component feedstock to obtain the needle coke, products such as coking dry gas, coking liquefied gas, coking gasoline, coking diesel, and coking wax oil can also be obtained.
[0087] It should be noted that when treating the second molecular component feedstock to obtain the second chemical product, all of the second molecular component feedstock can be pyrolyzed using the oil furnace process to produce carbon black; or all of the second molecular component feedstock can be pyrolyzed using the coking process to obtain the needle coke; or a part of the second molecular component feedstock can be used for pyrolysis using the oil furnace process, and another part of the second molecular component feedstock can be pyrolyzed using the coking process to obtain the second chemical product including carbon black and needle coke. That is, the embodiments of the present invention do not specifically limit the type of the second chemical product produced from the second molecular component feedstock, which can be selected according to actual needs.
[0088] In an optional embodiment, the heavy fraction oil processing method of the embodiments of the present invention, after obtaining the first chemical product, may further include: mixing the catalytic oil slurry included in the first chemical product with a viscosity-reducing liquid in a preset ratio to obtain a first mixture, and filtering the first mixture to remove solids to obtain a second mixture;
[0089] Using the second mixture to provide heat for the extraction treatment of the recycle oil, and pyrolyzing the second mixture to obtain the second chemical product;
[0090] Or,
[0091] Performing dearomatization treatment on the second mixture to obtain a third mixture and a fourth mixture, wherein the aromatic content of the fourth mixture is greater than that of the third mixture;
[0092] Performing pyrolysis treatment on the fourth mixture to obtain the second chemical product.
[0093] Since a large amount of heat is generated during the catalytic molecular reaction process, the temperature of the catalytic oil slurry obtained in step S101 is very high, and the high-temperature catalytic oil slurry can be used as one of the heat sources for the dearomatization treatment of the recycle oil, specifically as one of the heat sources for the solvent recovery tower.
[0094] Specifically, the catalytic slurry can be mixed with a viscosity-reducing liquid in a preset ratio to obtain a first mixture; wherein, the viscosity of the viscosity-reducing liquid is less than a preset threshold. The viscosity-reducing liquid can be a variety of liquids with relatively low viscosities, which are used to dilute the catalytic slurry.
[0095] Since the catalytic slurry contains a large amount of particulate matter (for example, catalyst particles, etc.), after obtaining the first mixture, a solid removal operation can be performed on the first mixture to obtain a catalytic slurry with better fluidity, that is, a second mixture, for subsequent processing.
[0096] Specifically, a filter, such as a ceramic membrane, can be used to perform cross-flow filtration on the first mixture under preset filtration conditions to obtain a second mixture; wherein, the preset filtration conditions may include: an operating temperature of 260°C to 350°C and a filtration pressure difference of 150 kPa to 200 kPa.
[0097] In the specific implementation process, the second mixture can be used to provide heat for the solvent recovery tower in various ways; for example: heat can be provided for the solvent recovery tower through the heat exchange operation between the second mixture and the bottom liquid of the extraction tower; or, the second mixture and the bottom liquid of the extraction tower can be mixed and injected into the solvent recovery tower to provide heat for the solvent recovery device.
[0098] Moreover, since the aromatic content in the catalytic slurry is relatively high, the second mixture can also be used together with the second molecular component feedstock for thermal cracking reaction to produce a second chemical product; the second mixture can also be subjected to dearomatization treatment to obtain a third mixture with a relatively low aromatic content and a fourth mixture with a relatively high aromatic content, and the fourth mixture can be used for thermal cracking reaction to produce a second chemical product, so as to make full use of the catalytic slurry. Optionally, when performing dearomatization treatment on the catalytic slurry, the second mixture can be mixed with recycle oil and enter the solvent extraction tower together for dearomatization treatment.
[0099] In an alternative embodiment, referring to Figure 3 As shown, taking the catalytic molecular reaction as the catalytic cracking reaction as an example, the overall process of the processing method of heavy distillate oil provided by the embodiments of the present invention is exemplarily described as follows:
[0100] The catalytic feedstock is added to a catalytic cracking reaction unit for catalytic cracking reaction to obtain recycle oil and first chemical products. The first chemical products include dry gas, liquefied gas, catalytic gasoline, catalytic diesel, recycle oil, catalytic slurry, etc. The recycle oil is fed into an extraction column for extraction treatment to obtain a first molecular component feedstock oil and an extraction bottom liquid. The first molecular component feedstock oil is added to the catalytic feedstock for catalytic cracking reaction together, while the extraction bottom liquid is fed into a solvent recovery column for separation treatment to separate out a second solvent and a second molecular component feedstock oil, and the second solvent is re-added to the extraction column for dearomatization treatment of the recycle oil.
[0101] The second molecular component feedstock oil is used as a material for producing carbon products such as carbon black and needle coke. And when separating the extraction bottom liquid, a second mixture obtained by mixing with a viscosity-reducing liquid and filtering through a filter can be fed into the extraction bottom liquid together to provide energy for the separation of the extraction bottom liquid.
[0102] The beneficial effects of the embodiments of the present application are illustrated below by taking the product yields obtained by processing the same heavy distillate oil using different process methods as shown in Table 2 as an example.
[0103] Among them, the density of the catalytic feedstock used is 903 kg / m 3 , the carbon residue is 4.1%, the catalytic molecular reaction temperature is 500 °C, the reaction pressure is 0.26 MPa, the catalyst-to-oil ratio is 7.2 during the reaction process, and the recycle ratio is 0.15, mainly producing products such as liquefied gas, gasoline, and diesel.
[0104] Among them, the comparative example is the product yield obtained by directly using the recycle oil produced by catalytic molecular reaction as the catalytic feedstock and then carrying out catalytic molecular reaction with the heavy distillate oil together.
[0105] Examples 1 and 2 are the product yields obtained by using the method provided by the embodiments of the present invention to carry out dearomatization treatment on the recycle oil obtained during the catalytic molecular reaction process, and then using the first molecular component feedstock oil after dearomatization treatment as the catalytic feedstock and carrying out catalytic molecular reaction with the heavy distillate oil together. Among them, when carrying out dearomatization treatment on the recycle oil, the first solvent used is a composite solvent with wet furfural as the main agent, the catalyst-to-oil ratio is 2.1, and the extraction temperature is 60 °C.
[0106] And in Example 1, after carrying out dearomatization treatment on the recycle oil, the obtained second molecular component feedstock oil and the second mixture obtained by carrying out viscosity reduction and solid removal treatment on the catalytic slurry are used together as the raw material for the carbon black unit to produce carbon black and by-products.
[0107] In Example 2, after the de-aromatization treatment of the recycle oil, the obtained second molecular component feedstock oil and the second mixture obtained after the viscosity reduction and solid removal treatment of the catalytic slurry oil are used together as the feedstock for the coking unit to produce needle coke and by-products.
[0108] Table 2
[0109] Serial number Item Comparative Example 1 Example 1 Example 2 1 Raw material yield (%) 100 100 100 2 Product yield (%) 99.9 99.7 99.5 2.1 Dry gas (%) 2.4 2.1 3.2 2.2 Liquefied gas (%) 20.5 19.4 19.6 2.3 Gasoline (%) 48.5 46.5 47.9 2.4 Light diesel oil (%) 16.9 15.0 17.2 2.5 Slurry oil (%) 3.5 － － 2.6 Coking (%) 8.1 5.4 5.4 2.7 Carbon black (%) － 6.5 － 2.8 By-products such as hydrogen (%) － 4.8 － 2.9 Needle coke before calcination (%) － － 6.2
[0110] As shown in Table 2, compared with the above Comparative Example 1, in Example 1 and Example 2, the charring rate of the catalytic molecular reaction is reduced by 2.7 percentage points compared with the charring rate of the catalytic molecular reaction in Comparative Example 1, effectively reducing carbon emissions. At the same time, high-value high-end carbon products such as carbon black and needle coke can also be obtained. It can be seen from Table 2 that the yield of the carbon black product produced in Example 1 is 6.5%, and the yield of the needle coke product produced in Example 2 is 6.2%. That is, by using the heavy oil fractionation processing method provided by the embodiments of the present invention, while effectively reducing the charring rate of the catalytic molecular reaction, the diversification of chemical products from heavy distillate oil can be realized.
[0111] Furthermore, under different extraction conditions, the first molecular component feedstock oil with different aromatic hydrocarbon contents is obtained after processing the recycle oil, and when the first molecular component feedstock oil is added to the catalytic molecular reaction, the catalytic charring rate of the catalytic molecular reaction is shown in Comparative Example 2, Comparative Example 3, Example 3, Example 4 and Example 5 in Table 3; among them, the density of the recycle oil is 0.98 g·mL -1 , and the aromatic hydrocarbon content is 69%.
[0112] Table 3
[0113]
[0114] It can be seen from the above Table 3 that when the recycle oil is subjected to aromatic hydrocarbon treatment, when the first solvent is furfural solvent and the reaction conditions are an extraction temperature of 60°C to 100°C and a solvent-to-oil ratio of 2 to 3, compared with the reaction conditions where the temperature of the de-aromatization treatment is less than 60°C and the solvent-to-oil ratio is less than 2, the catalytic charring rate decreases somewhat; and referring to Table 3 and Figure 2As shown in the figure, the inventors of the present application found in experiments that under the reaction conditions where the temperature is higher than 100°C and the catalyst-oil ratio is greater than 3, compared with the temperature of 100°C and the catalyst-oil ratio of 3, the aromatic hydrocarbon content of the first molecular component feedstock obtained by extraction is similar, and after catalytic molecular reaction treatment, the catalytic coking rate generated is also similar. That is, when performing dearomatization treatment on recycle oil, under the reaction conditions where the reaction temperature is higher than 100°C and the catalyst-oil ratio is higher than 3, the extraction separation effect will not be significantly improved, but more energy waste will be caused due to the increase in temperature and catalyst-oil ratio. Therefore, it can be concluded that when performing dearomatization treatment on recycle oil, the extraction agent is furfural solution, the reaction temperature is 60°C to 100°C, and the catalyst-oil ratio is 2 to 3, the extraction effect is better, and the effect of reducing the catalytic coking rate is also better.
[0115] Optionally, when performing dearomatization treatment on recycle oil, the extraction agent used can be furfural solvent, or other extraction agents that can perform extraction treatment on recycle oil. The embodiments of the present invention do not make specific limitations on this, and can be selected according to actual needs. For example, it can also be a mixed solvent obtained by mixing one or more solvents among furfural solvent, N-methylpyrrolidone, and N,N-dimethylformamide.
[0116] Further, after obtaining the second molecular component feedstock, using the oil furnace process, under the first preset pyrolysis conditions, the obtained second molecular component feedstock is pyrolyzed to obtain carbon black. During the process, under different first preset pyrolysis conditions, taking the pyrolysis process of the second molecular component feedstock with an aromatic hydrocarbon content of 87% as an example, the yield of the obtained carbon black product is shown in Comparative Example 4, Comparative Example 5, Example 6, and Example 7 in Table 3 below;
[0117] Table 4
[0118] Serial number Comparative Example 3 Example 6 Example 7 Comparative Example 4 One Reaction conditions Oxygen content 21％ 23％ 28％ 21％ Reaction temperature, °C 1750 1750 1930 1930 Total combustion rate 26 26 26 26 Two Carbon black yield Hard carbon black 47.9 46.6 Soft carbon black 55.5 56.3
[0119] When pyrolyzing the second molecular component feedstock, when the reaction temperature is 1750°C, the carbon black product produced is soft carbon black. It can be seen from Table 4 that at the same temperature, when the oxygen content in the air is lower than 23%, compared with the case where the oxygen content in the air is 23%, the content of the produced soft carbon black will decrease; when pyrolyzing the second molecular component feedstock, when the reaction temperature is 1930°C, the carbon black product produced is hard carbon black, and at the same temperature, under the reaction conditions with a lower oxygen content, the content of carbon black decreases.
[0120] It can be known that under the reaction conditions between the production of soft carbon black and hard carbon black, the product of pyrolyzing the second molecular component feedstock is hard carbon black or soft carbon black. And when pyrolyzing the second molecular component feedstock with the same content, the obtained product, hard carbon black or soft carbon black, has a higher carbon black content compared to carbon black with a lower oxygen content. Therefore, when pyrolyzing the second molecular component feedstock, the reaction temperature is 1750°C - 1930°C, the total combustion rate is 26%, and the oxygen content in the air is in the range of 23% - 28%, which is more conducive to improving the overall yield of carbon black. And the inventors of the present application carried out corresponding treatments on the second molecular component feedstock with other aromatic hydrocarbon contents and found that the pattern is similar.
[0121] The heavy fraction oil processing method provided by the embodiments of the present invention performs catalytic molecular reaction treatment on the catalytic feedstock to obtain recycle oil and a first chemical product; wherein, the catalytic feedstock includes: the heavy fraction oil to be processed; the recycle oil is subjected to dearomatization treatment to obtain a first molecular component feedstock and a second molecular component feedstock; the first molecular component feedstock with a lower aromatic hydrocarbon content is returned to the catalytic feedstock for catalytic molecular reaction treatment, thereby effectively reducing the catalytic coking rate in the catalytic molecular reaction process, reducing carbon emissions, and being able to alleviate the problem that a large amount of coke products generated under a higher coking rate block the catalytic molecular reaction device, resulting in the inability of the device to operate in a long cycle; and the second molecular component feedstock rich in aromatic components is pyrolyzed to obtain a second chemical product including at least one of carbon black and needle coke, realizing the diversification of products produced from heavy fraction oil and the high-value utilization of recycle oil.
[0122] Based on the same inventive concept, referring to Figure 4 As shown, the embodiments of the present invention also provide a heavy fraction oil processing system 200, including: a catalytic molecular reaction device 210 and a dearomatization treatment device 220;
[0123] The catalytic molecular reaction device 210 is used to perform catalytic molecular reaction treatment on the catalytic feedstock to obtain recycle oil and a first chemical product; the catalytic feedstock includes: the heavy fraction oil to be processed; and it is used to continue the catalytic molecular reaction treatment with the first molecular component feedstock obtained from the dearomatization treatment device and the heavy fraction oil to be processed as the catalytic feedstock;
[0124] The dearomatization treatment device 220 is used to perform dearomatization treatment on the recycle oil obtained from the catalytic molecular reaction device to obtain a first molecular component feedstock and a second molecular component feedstock; wherein, the aromatic hydrocarbon content of the first molecular component feedstock is less than a first preset threshold, the aromatic hydrocarbon content of the second molecular component feedstock is greater than a second preset threshold, and the second preset threshold is greater than the first preset threshold.
[0125] Optionally, the heavy fraction oil processing system 200 provided by the embodiments of the present invention may further include: a thermal cracking device;
[0126] The thermal cracking device is used to perform thermal cracking treatment on the second molecular component feedstock obtained from the dearomatization treatment device to obtain second chemical products;
[0127] Wherein, the second chemical products include at least one of carbon black and needle coke.
[0128] Further, in the heavy fraction oil processing system provided by the embodiments of the present invention, the dearomatization treatment may include: an extraction tower and a solvent recovery tower;
[0129] Wherein, the extraction tower is used to perform extraction treatment on the recycle oil with a first solvent under preset extraction conditions to obtain a first molecular component feedstock and an extraction bottom liquid;
[0130] The solvent recovery tower is used to perform separation treatment on the extraction bottom liquid to obtain a second grouped component feedstock and a second solvent.
[0131] Further, the heavy fraction oil processing system provided by the embodiments of the present invention may further include: a filter, which is used to perform solid removal filtration on the first mixture to obtain a second mixture.
[0132] Regarding the heavy fraction oil processing system in the above embodiments, the specific manners and beneficial effects of each module performing operations have been described in detail in the embodiments related to the method, and will not be elaborated here.
[0133] The basic concepts have been described above. Obviously, for those skilled in the art, the above detailed disclosure is only an example and does not constitute a limitation to this application. Although not explicitly stated here, those skilled in the art may make various modifications, improvements, and corrections to this application. Such modifications, improvements, and corrections are proposed in this application, so such modifications, improvements, and corrections still belong to the spirit and scope of the exemplary embodiments of this application.
[0134] At the same time, specific terms are used in this application to describe the embodiments of this application. Such as "one embodiment", "an embodiment", and / or "some embodiments" mean a certain feature, structure, or characteristic related to at least one embodiment of this application. Therefore, it should be emphasized and noted that "an embodiment" or "one embodiment" or "an alternative embodiment" mentioned twice or more at different positions in this application does not necessarily refer to the same embodiment. In addition, certain features, structures, or characteristics in one or more embodiments of this application can be appropriately combined.
[0135] In addition, unless clearly stated in the claims, the order of the processing elements and sequences, the use of numerical and alphabetical characters, or the use of other names in this application are not used to limit the order of the processes and methods of this application. Although some currently useful embodiments of the invention are discussed through various examples in the above disclosure, it should be understood that such details are only for illustrative purposes. The appended claims are not limited to the disclosed embodiments. On the contrary, the claims are intended to cover all modifications and equivalent combinations that conform to the essence and scope of the embodiments of this application. For example, although the system components described above can be implemented by hardware devices, they can also be implemented only through software solutions, such as installing the described system on existing servers or mobile devices.
[0136] Similarly, it should be noted that, in order to simplify the presentation of the disclosure of this application and thus help the understanding of one or more embodiments of the invention, in the previous description of the embodiments of this application, sometimes multiple features are merged into one embodiment, drawing, or description thereof. However, this method of disclosure does not mean that the features required by the subject matter of this application are more than those mentioned in the claims. In fact, the features of the embodiments are less than all the features of the individual embodiments disclosed above.
[0137] In some embodiments, numbers are used to describe the components and the quantity of attributes. It should be understood that such numbers used to describe the embodiments are modified by the modifiers "about", "approximate" or "substantially" in some examples. Unless otherwise stated, "about", "approximate" or "substantially" indicate that the stated numbers allow a variation of ±20%. Accordingly, in some embodiments, the numerical parameters used in the specification and claims are approximate values, and these approximate values can be changed according to the characteristics required by individual embodiments. In some embodiments, the numerical parameters should consider the specified significant digits and adopt the method of retaining the general number of digits. Although the numerical ranges and parameters used in some embodiments of this application to confirm the breadth of their scope are approximate values, in specific embodiments, the setting of such numerical values is as precise as possible within the feasible range.
[0138] For each patent, patent application, patent application publication, and other materials cited in this application, such as articles, books, specifications, publications, documents, etc., their entire contents are hereby incorporated into this application by reference. Except for the application history documents that are inconsistent with or conflict with the content of this application, and except for the documents that limit the broadest scope of the claims of this application (currently or subsequently appended to this application). It should be noted that if there are inconsistencies or conflicts between the descriptions, definitions, and / or uses of terms in the attached materials of this application and the content described in this application, the descriptions, definitions, and / or uses of terms in this application shall prevail.
Claims
1. A method for processing heavy distillate oil, characterized in that, Comprising: Performing catalytic molecular reaction treatment on a catalytic feedstock to obtain recycle oil and a first chemical product; The catalytic feedstock includes: heavy distillate oil to be processed; Performing dearomatization treatment on the recycle oil to obtain a first molecular component feedstock oil and a second molecular component feedstock oil; wherein, the aromatic content of the first molecular component feedstock oil is less than a first preset threshold, the aromatic content of the second molecular component feedstock oil is greater than a second preset threshold, and the second preset threshold is greater than the first preset threshold; Adding the first molecular component feedstock oil to the catalytic feedstock and continuing to perform catalytic molecular reaction treatment.
2. The heavy fraction oil processing method according to claim 1, wherein, Performing dearomatization treatment on the recycle oil to obtain a first molecular component feedstock oil and a second molecular feedstock oil, including: using a first solvent to perform extraction treatment on the recycle oil under preset extraction conditions to obtain a first molecular component feedstock oil and a second molecular feedstock oil.
3. The heavy fraction oil processing method according to claim 2, wherein Using a first solvent to perform extraction treatment on the recycle oil under preset extraction conditions to obtain a first molecular component feedstock oil and a second molecular component feedstock oil, including: Using a first solvent to perform extraction treatment on the recycle oil under preset extraction conditions to obtain the first molecular component feedstock oil and an extraction bottoms liquid; Performing separation treatment on the extraction bottoms liquid to separate out a second grouped component feedstock oil and a second solvent.
4. The heavy fraction oil processing method according to claim 2, characterized in that, The preset extraction conditions include: temperature 60°C to 100°C, solvent-to-oil ratio 2 to 3.
5. The heavy fraction oil processing method according to claim 1, characterized in that, Also including: Performing thermal cracking treatment on the second molecular component feedstock oil to obtain a second chemical product; The second chemical product includes: at least one of carbon black and needle coke.
6. The heavy fraction oil processing method according to claim 5, characterized in that, Performing thermal cracking treatment on the second molecular component feedstock oil to obtain a second chemical product, including: Adopting an oil furnace process to perform thermal cracking treatment on the second molecular component feedstock oil under first preset thermal cracking conditions to obtain the carbon black; And / or, Adopting a coking process to perform thermal cracking treatment on the second molecular component feedstock oil under second preset thermal cracking conditions to obtain the needle coke.
7. The heavy fraction oil processing method according to claim 6, characterized in that, The first preset thermal cracking conditions include: the reaction temperature range is 1750°C to 1930°C, the oxygen content of the air participating in the thermal cracking reaction is in the range of 23% - 28%, and the total combustion rate is 26%.
8. The heavy fraction oil processing method according to claim 1, characterized in that, The catalytic molecular reaction is a catalytic cracking reaction or a catalytic pyrolysis reaction.
9. The heavy fraction oil processing method according to claim 6, characterized in that, Also including: Mixing the catalytic slurry included in the first chemical product with a viscosity-reducing liquid in a preset ratio to obtain a first mixture, and performing solid removal by filtration on the first mixture to obtain a second mixture; Using the second mixture to provide heat for the extraction treatment of the recycle oil, and performing thermal cracking treatment on the second mixture to obtain a second chemical product; Or, Performing dearomatization treatment on the second mixture to obtain a third mixture and a fourth mixture, wherein the aromatic content of the fourth mixture is greater than that of the third mixture; Performing thermal cracking treatment on the fourth mixture to obtain a second chemical product.
10. A processing system for heavy distillate oil, characterized in that, Including: A catalytic molecular reaction device, a dearomatization treatment device; The catalytic molecular reaction device is used for carrying out catalytic molecular reaction treatment on catalytic raw materials to obtain recycled oil and a first chemical product; the catalytic raw materials include: heavy fraction oil to be processed; and the first molecular component raw oil obtained from the dearomatization treatment device is used together with the heavy fraction oil to be processed as catalytic raw materials to continue the catalytic molecular reaction treatment; The dearomatization treatment device is used for carrying out dearomatization treatment on the recycled oil obtained from the catalytic molecular reaction device to obtain a first molecular component raw oil and a second molecular component raw oil; wherein, the aromatic hydrocarbon content of the first molecular component raw oil is less than a first preset threshold value, the aromatic hydrocarbon content of the second molecular component raw oil is greater than a second preset threshold value, and the second preset threshold value is greater than the first preset threshold value.
11. The processing system according to claim 10, characterized in that, It further includes: A thermal cracking device; The thermal cracking device is used for carrying out thermal cracking treatment on the second molecular component raw oil obtained from the dearomatization treatment device to obtain a second chemical product; The second chemical product includes at least one of carbon black and needle coke.
12. The processing system according to claim 11, wherein, The dearomatization treatment device includes an extraction tower and a solvent recovery tower; The extraction tower is used for using a first solvent to carry out extraction treatment on the recycled oil obtained from the catalytic molecular reaction device under preset extraction conditions to obtain the first molecular component raw oil and extraction bottom liquid; The solvent recovery tower is used for carrying out separation treatment on the extraction bottom liquid to obtain a second grouped component raw oil and a second solvent.