A synergistic processing system for inferior residual oil

Abstract

The utility model discloses a kind of collaborative processing systems of inferior residual oil, comprising: DCC unit, olefin polymer unit, carbon black production unit, aromatic hydrocarbon combined unit, MTBE synthesis unit, butadiene preparation unit and rubber synthesis unit;Wherein, the outlet of the DCC unit is connected with the inlet of the olefin polymer unit, the carbon black production unit, the aromatic hydrocarbon combined unit and the MTBE synthesis unit respectively;The outlet of the MTBE synthesis unit is connected with the inlet of the butadiene preparation unit, the outlet of the butadiene preparation unit is connected with the inlet of the rubber synthesis unit;The outlet of the aromatic hydrocarbon combined unit is connected with the inlet of the rubber synthesis unit;The utility model is by the technical integration and collaborative processing of each unit, finally realizes the total resource utilization of inferior residual oil, to improve its economic value.

Description

Technical Field

[0001] This utility model relates to the field of petrochemical technology, specifically to a co-processing system for inferior residual oil. Background Technology

[0002] Low-quality residual oil is a heavy residue left over from crude oil during primary processing such as atmospheric and vacuum distillation and catalytic cracking. It usually refers to vacuum residue or even heavier oil products. It is characterized by high impurity content, high density, high viscosity, complex molecular structure, and is rich in sulfur, nitrogen, metallic impurities, and asphaltenes, making it one of the most difficult components to process in refineries.

[0003] The efficient utilization of low-quality residual oil is crucial for improving the utilization rate of crude oil resources and the economic benefits of refineries. Existing technologies utilize catalytic cracking techniques such as DCC (Catalytic Thermal Cracking of Residue Oil), which, through high temperatures and the action of specialized catalysts, cracks large-molecule hydrocarbons (such as long-chain alkanes and aromatics) in low-quality residual oil into smaller-molecule hydrocarbons. This primarily produces high-value-added low-carbon olefins (ethylene, propylene), light oil products (naphtha, diesel), and gaseous products (hydrogen-rich gas, dry gas, etc.).

[0004] However, the oil products obtained by cracking inferior residual oil using DCC technology are unsuitable for direct use as blending components in gasoline and diesel fuel due to their high aromatic content. Furthermore, the value of aromatics is not fully realized, resulting in low economic benefits. In addition, the inherent limitations of DCC technology lead to higher impurity content in the cracked products, resulting in lower market prices and further reducing the company's economic efficiency. Utility Model Content

[0005] To achieve the above objectives, this utility model provides the following technical solution: a co-processing system for inferior residual oil, comprising: a DCC unit, an olefin polymer unit, a carbon black production unit, an aromatic hydrocarbon complex unit, an MTBE synthesis unit, a butadiene preparation unit, and a rubber synthesis unit; The outlet of the DCC unit is connected to the inlet of the olefin polymer unit, the carbon black production unit, the aromatic hydrocarbon complex unit, and the MTBE synthesis unit, respectively. The outlet of the MTBE synthesis unit is connected to the inlet of the butadiene preparation unit, and the outlet of the butadiene preparation unit is connected to the inlet of the rubber synthesis unit. The outlet of the aromatic hydrocarbon complex unit is connected to the inlet of the rubber synthesis unit; The DCC unit includes: a steam cracking reactor, a fractionation tower, a cracked gas compressor, an impurity removal device, and a cryogenic separation system; The steam cracking reactor, the fractionation tower, the cracked gas compressor, the impurity removal device, and the cryogenic separation system are connected in series and configured to produce polymer-grade ethylene and polymer-grade propylene from inferior residue oil, and to produce byproducts such as hydrogen-rich gas, methane hydrogen, mixed C4, cracked naphtha, cracked light oil, and cracked heavy oil.

[0006] Furthermore, as a preferred embodiment, the fractionation tower includes: a cracked gas production outlet, a cracked naphtha production outlet, a cracked light oil discharge outlet, and a cracked heavy oil discharge outlet; The fractionation tower is provided with a cracked gas production outlet and a cracked naphtha production outlet at the top of the tower, a cracked light oil discharge outlet at the side of the fractionation tower, and a cracked heavy oil discharge outlet at the bottom of the fractionation tower. The cracked gas extraction outlet is connected to the inlet of the cracked gas compressor via a material pipe, and the cracked naphtha extraction outlet and the cracked light oil discharge outlet are both connected to the feed inlet of the aromatics complex unit via material pipes. The pyrolysis heavy oil outlet is connected to the carbon black production unit inlet via a material pipe.

[0007] Furthermore, as a preferred embodiment, the olefin polymer unit includes a polyethylene production line and a polypropylene production line arranged in parallel, and the feed inlet of the olefin polymer unit is connected to the discharge outlets of the polymer-grade ethylene and polymer-grade propylene of the DCC unit through material pipes, respectively. The carbon black production unit includes a high-temperature pyrolysis reactor, a quench collection system, and a pretreatment device. The aromatics complex unit includes a hydrogenation system and an aromatics separation system. The feed inlet of the aromatics complex unit is connected to the cracked naphtha production outlet, cracked light oil discharge outlet, methane hydrogen discharge outlet and hydrogen-rich gas discharge outlet of the DCC unit through a material pipe. The MTBE synthesis unit includes a hydrogenation reactor and an MTBE reactive distillation column arranged in series. The feed inlet of the MTBE synthesis unit is connected to the discharge outlet of the mixed C4 of the DCC unit through a material pipe. The discharge outlet of the MTBE synthesis unit is connected to the inlet of the butadiene preparation unit through a material pipe. The butadiene preparation unit includes a dehydrogenation reactor, an isomerization reactor, and a product separation tower connected in sequence. The outlet of the butadiene preparation unit is connected to the inlet of the rubber synthesis unit through a material pipe. The rubber synthesis unit includes a butadiene rubber production line and a styrene-butadiene rubber production line arranged in parallel. The feed inlet of the rubber synthesis unit is connected to the discharge outlet of the butadiene preparation unit and the aromatic hydrocarbon combination unit through material pipes, respectively.

[0008] Furthermore, as a preferred embodiment, the cryogenic separation system includes: a demethanizer, a deethaner, an ethylene distillation column, a depropanizer, and a propylene distillation column; The demethanizer inlet is connected to the impurity removal unit outlet, the top of the demethanizer is connected to the aromatics complex inlet via a pipeline, and the bottom of the demethanizer is connected to the deethaner inlet via a pipeline. The top of the deethanizer is connected to the inlet of the ethylene distillation column via a pipeline, and the bottom of the deethanizer is connected to the inlet of the depropanizer via a pipeline; The top of the ethylene distillation column is connected to the feed inlet of the olefin polymer unit via a pipeline, and the bottom of the ethylene distillation column is connected to the inlet of the steam cracking reactor via a pipeline. The top of the depropanizer is connected to the inlet of the propylene distillation column via a pipeline, and the bottom of the depropanizer is connected to the inlet of the MTBE synthesis unit via a pipeline; The top of the propylene distillation column is connected to the feed inlet of the olefin polymer unit via a pipeline, and the bottom of the propylene distillation column is connected to the inlet of the steam cracking reactor via a pipeline.

[0009] Furthermore, as a preferred embodiment, the hydrogenation system includes: a hydrogenation refining unit, a hydrogen purification unit, a hydrogenation reforming unit, and an extraction unit; The hydrorefining unit is used to hydrorefine pyrolyzed naphtha, the hydromodification unit is used to hydromodify pyrolyzed light oil, the hydrogen purification unit is used to separate high-purity hydrogen, and the extraction unit is used to perform liquid-liquid extraction. The outlet of the hydrogen purification unit is connected to the inlet of the hydrorefining unit and the hydromodification unit. The inlet of the extraction unit is connected to the outlet of the hydrorefining unit and the hydromodification unit through a material pipe. The outlet of the extraction unit is connected to the inlet of the aromatics separation system through a material pipe.

[0010] Furthermore, as a preferred embodiment, the aromatic hydrocarbon separation system includes: a heavy aromatic hydrocarbon adsorption and separation module and a desorption module; The inlet of the desorption module is connected to the outlet of the hydrorefining unit, the hydromodification unit, and the heavy aromatics adsorption and separation module via a pipeline, and the outlet of the desorption module is connected to the inlet of the rubber synthesis unit via a material pipe.

[0011] Furthermore, as a preferred embodiment, the outlet of the extraction unit is connected to the feed inlet of the steam cracking reactor of the DCC unit via a pipeline to form a closed loop.

[0012] Furthermore, as a preferred embodiment, the top outlet of the MTBE reactive distillation column is connected to the feed inlet of the steam cracking reactor via a pipeline, the upper outlet of the MTBE reactive distillation column is connected to the inlet of the dehydrogenation reactor via a pipeline, and the outlet of the dehydrogenation reactor is connected to the inlet of the rubber synthesis unit via a pipeline.

[0013] Furthermore, as a preferred embodiment, the styrene-butadiene rubber production line includes: a styrene production unit, a separator, and a polymerization unit; The outlet of the styrene production unit is connected to the inlet of the separator via a pipe, and the outlet of the separator is connected to the inlets of both the styrene production unit and the polymerization unit via pipes.

[0014] Furthermore, as a preferred embodiment, it also includes: a copolymerization reactor; The inlet of the hydrogenation reactor is connected to the outlet of the butadiene preparation unit via a pipeline, and the inlet of the copolymerization reactor is connected to the outlet of the hydrogenation reactor and the outlet of the polymerization-grade ethylene of the DCC unit via pipelines.

[0015] Compared with the prior art, this utility model provides a co-processing system for inferior residual oil, which has the following beneficial effects: Advantage 1: This utility model, through the technical integration and collaborative processing of various units, ultimately achieves the complete resource utilization of inferior residual oil, thereby increasing its economic value. It effectively solves the problem that existing processing methods for inferior residual oil do not fully reflect its value and have low economic benefits. Furthermore, based on the existing industry, it systematically plans the remaining products from inferior residual oil processing, determines processing and utilization pathways according to product characteristics, completes the inferior residual oil processing industrial chain, and improves the economic benefits of enterprises. Attached Figure Description

[0016] Figure 1 A schematic diagram of a co-processing system for low-quality residual oil. Figure 1 ; Figure 2 A schematic diagram of the DCC unit structure of a co-processing system for low-quality residual oil; Figure 3 A schematic diagram of the structure of a co-processing system for low-quality residual oil, consisting of a hydrogenation system and an aromatics separation system; Figure 4 A schematic diagram of the MTBE synthesis unit structure in a co-processing system for low-quality residual oil; Figure 5 A schematic diagram of the butadiene preparation unit structure in a co-processing system for low-quality residual oil; Figure 6 A schematic diagram of a styrene-butadiene rubber production line for the co-processing of low-quality residual oil; Figure 7A schematic diagram of the olefin polymer unit structure of a co-processing system for low-quality residual oil; Figure 8 A schematic diagram of the carbon black production unit structure in a co-processing system for low-quality residual oil; Figure 9 A schematic diagram of a co-processing system for low-quality residual oil. Figure 2 ; In the diagram: 1. DCC unit; 11. Steam cracking reactor; 12. Fractionating tower; 121. Cracking gas outlet; 122. Cracking naphtha outlet; 123. Cracking light oil outlet; 124. Cracking heavy oil outlet; 13. Cracking gas compressor; 14. Impurity removal device; 15. Cryogenic separation system; 151. Methanogen remover; 152. Ethane remover; 153. Ethylene distillation tower; 154. Propane remover; 155. Propylene distillation tower; 2. Olefin polymer unit; 21. Polyethylene production line; 22. Polypropylene production line; 3. Carbon black production unit; 31. High-temperature cracking reactor; 32. Quenching collection system; 33. Pretreatment device; 4. Aromatic Hydrocarbon complex unit; 41. Hydrogenation system; 411. Hydrogenation refining unit; 412. Hydrogen purification unit; 413. Hydrogenation reforming unit; 414. Extraction unit; 42. Aromatic hydrocarbon separation system; 421. Heavy aromatic hydrocarbon adsorption and separation module; 422. Desorption module; 5. MTBE synthesis unit; 51. Hydrogenation reactor; 52. MTBE reactive distillation column; 6. Butadiene preparation unit; 61. Dehydrogenation reactor; 62. Isomerization reactor; 63. Product separation column; 7. Rubber synthesis unit; 71. Butadiene rubber production line; 72. Styrene-butadiene rubber production line; 721. Styrene production unit; 722. Separator; 723. Polymerization unit; 8. Copolymerization reactor. Detailed Implementation

[0017] Please see Figures 1-9 This utility model provides a co-processing system for inferior residual oil, including: DCC unit 1, olefin polymer unit 2, carbon black production unit 3, aromatic hydrocarbon complex unit 4, MTBE synthesis unit 5, butadiene preparation unit 6, and rubber synthesis unit 7. The outlet of DCC unit 1 is connected to the inlet of olefin polymer unit 2, carbon black production unit 3, aromatic hydrocarbon complex unit 4 and MTBE synthesis unit 5, respectively. The outlet of the MTBE synthesis unit 5 is connected to the inlet of the butadiene preparation unit 6, and the outlet of the butadiene preparation unit 6 is connected to the inlet of the rubber synthesis unit 7. The outlet of the aromatic hydrocarbon complex unit 4 is connected to the inlet of the rubber synthesis unit 7; The DCC unit 1 includes: a steam cracking reactor 11, a fractionation tower 12, a cracked gas compressor 13, an impurity removal device 14, and a cryogenic separation system 15; The steam cracking reactor 11, the fractionation tower 12, the cracked gas compressor 13, the impurity removal device 14, and the cryogenic separation system 15 are connected in series and configured to produce polymer-grade ethylene and polymer-grade propylene from inferior residue oil, and to produce byproducts such as hydrogen-rich gas, methane hydrogen, mixed C4, cracked naphtha, cracked light oil, and cracked heavy oil.

[0018] It is important to note that, such as Figure 1 The structure shown is merely one example of the present invention and does not represent the only possible structure for a co-processing system for inferior residual oil. The final result can be achieved through various methods. Figure 1 The structure shown can be modified and transformed in various ways.

[0019] Furthermore, the fractionation tower 12 includes: a cracked gas extraction outlet 121, a cracked naphtha extraction outlet 122, a cracked light oil discharge outlet 123, and a cracked heavy oil discharge outlet 124. The fractionation tower 12 is provided with a cracked gas production outlet 121 and a cracked naphtha production outlet 122 at the top of the tower, a cracked light oil discharge outlet 123 at the side of the fractionation tower 12, and a cracked heavy oil discharge outlet 124 at the bottom of the fractionation tower 12. The cracked gas outlet 121 is connected to the inlet of the cracked gas compressor 13 through a material pipe to compress the cracked gas. The cracked naphtha outlet 122 and the cracked light oil outlet 123 are both connected to the feed port of the aromatics complex unit 4 through material pipes. In this embodiment, the cracked gas includes hydrogen-rich gas, ethylene, propylene, methane hydrogen, and mixed C4.

[0020] The pyrolysis heavy oil outlet 124 is connected to the inlet of the carbon black production unit 3 via a material pipe.

[0021] Furthermore, the olefin polymer unit 2 includes a polyethylene production line 21 and a polypropylene production line 22 arranged in parallel. The feed inlet of the olefin polymer unit 2 is connected to the discharge outlets of the polymer-grade ethylene and polymer-grade propylene of the DCC unit 1 through material pipes, respectively. The carbon black production unit 3 includes a high-temperature pyrolysis reactor 31, a quench collection system 32, and a pretreatment device 33. In this embodiment, the pretreatment device 33 is used to remove mechanical impurities from the pyrolysis heavy oil and also to adjust the viscosity of the pyrolysis heavy oil.

[0022] In a preferred embodiment, the pretreatment device 33 is specifically used to remove solid particles (such as coke powder, catalyst residue, and metal shavings), gums, and asphalt lumps from the pyrolysis heavy oil, preventing blockage or wear in downstream equipment. It can also reduce the viscosity of the pyrolysis heavy oil to meet the flowability requirements of equipment such as transfer pumps and heat exchangers.

[0023] The aromatics complex unit 4 includes a hydrogenation system 41 and an aromatics separation system 42. The feed inlet of the aromatics complex unit 4 is connected to the cracked naphtha outlet 122, the cracked light oil outlet 123, the methane hydrogen outlet and the hydrogen-rich gas outlet of the DCC unit 1 through a material pipe. The MTBE synthesis unit 5 includes a hydrogenation reactor 51 and an MTBE reactive distillation column 52 arranged in series. The feed inlet of the MTBE synthesis unit 5 is connected to the discharge outlet of the mixed C4 of the DCC unit 1 through a material pipe. The discharge outlet of the MTBE synthesis unit 5 is connected to the inlet of the butadiene preparation unit 6 through a material pipe. The butadiene preparation unit 6 includes a dehydrogenation reactor 61, an isomerization reactor 62 and a product separation tower 63 connected in sequence. The outlet of the butadiene preparation unit 6 is connected to the inlet of the rubber synthesis unit 7 through a material pipe. The rubber synthesis unit 7 includes a butadiene rubber production line 71 and a styrene-butadiene rubber production line 72 arranged in parallel. The feed inlet of the rubber synthesis unit 7 is connected to the discharge outlet of the butadiene preparation unit 6 and the aromatic hydrocarbon combination unit 4 through a material pipe.

[0024] Furthermore, the cryogenic separation system 15 includes: a demethanizer 151, a deethaner 152, an ethylene distillation column 153, a depropanizer 154, and a propylene distillation column 155; The inlet of the demethanizer 151 is connected to the outlet of the impurity removal device 14, the top of the demethanizer 151 is connected to the inlet of the aromatic hydrocarbon complex unit 4 through a pipeline, and the bottom of the demethanizer 151 is connected to the inlet of the deethaner 152 through a pipeline. In this embodiment, the demethanizer 151 is used to separate methane hydrogen from the low-temperature cracked gas from the impurity removal unit 14, and send the methane hydrogen to the aromatics complex unit 4 through a pipeline at the top of the tower, and input the bottom product into the deethanizer 152.

[0025] The top of the deethanizer 152 is connected to the inlet of the ethylene distillation column 153 via a pipeline, and the bottom of the deethanizer 152 is connected to the inlet of the depropanizer 154 via a pipeline; In this embodiment, the deethaner 152 is used to separate the C2 and C3 fractions from the bottom product of the demethanizer 151. The ethane and ethylene mixture collected from the top of the column is fed into the ethylene distillation column 153, and the bottom product is fed into the depropanizer 154.

[0026] The top of the ethylene distillation column 153 is connected to the feed inlet of the olefin polymer unit 2 via a pipeline, and the bottom of the ethylene distillation column 153 is connected to the inlet of the steam cracking reactor 11 via a pipeline; In this embodiment, the ethylene distillation column 153 is used to separate polymer-grade ethylene from the mixture of ethane and ethylene, and feed it from the top of the column into the feed inlet of the olefin polymer unit 2, while the ethane at the bottom of the column is recycled back to the steam cracking reactor 11.

[0027] The top of the depropanizer 154 is connected to the inlet of the propylene distillation column 155 via a pipeline, and the bottom of the depropanizer 154 is connected to the inlet of the MTBE synthesis unit 5 via a pipeline. In this embodiment, the propane depropanizer 154 is used to separate a mixture of propylene and propane from the bottom product of the ethane depropanizer 152 and feed it from the top of the column into the propylene distillation column 155. The mixed C4 and cracked naphtha at the bottom of the column are fed into the MTBE synthesis unit 5.

[0028] The top of the propylene distillation column 155 is connected to the feed inlet of the olefin polymer unit 2 via a pipeline, and the bottom of the propylene distillation column 155 is connected to the inlet of the steam cracking reactor 11 via a pipeline.

[0029] In this embodiment, the propylene distillation column 155 is used to separate polymer-grade propylene from the propylene and propane mixture and feed it from the top of the column into the feed port of the olefin polymer unit 2, while the propane at the bottom of the column is recycled back to the steam cracking reactor 11.

[0030] In a preferred embodiment, specifically, the demethanizer 151 operates under cryogenic conditions (e.g., -100°C) to separate the cryogenic cracked gas into a mixture of hydrogen and methane (methane hydrogen) at the top and C2 and higher weight components at the bottom. The product from the top is further cooled and separated to produce hydrogen-rich gas, while the remaining methane hydrogen is sent to the aromatics complex 4 as fuel or a hydrogen source. The bottom temperature of the demethanizer 151 is controlled at -50 to -20°C to prevent C2 components from entering the top. The bottom product is pressurized by a pump and sent to the deethanizer 152.

[0031] Deethanizer 152 separates light and heavy components from the bottom product of demethanizer 151. The top gas from deethanizer 152 (including ethane and ethylene) is partially refluxed after condensation, with the remainder sent to ethylene distillation column 153. The bottom temperature of deethanizer 152 is controlled at 70–90°C to prevent C3 from entering the top and affecting ethylene purity. The bottom product of deethanizer 152 (containing propylene, propane, C4+, etc.) is sent to depropanizer 154.

[0032] In ethylene distillation column 153, a mixture of ethane and ethylene is distilled and purified to polymer-grade ethylene (≥99.95% purity). The polymer-grade ethylene gas collected from the top of ethylene distillation column 153 is dehydrated in a dryer and sent to olefin polymer unit 2 as a feedstock. The bottom product of ethylene distillation column 153 is high-purity ethane, which can be heated in a reboiler and recycled back to steam cracking reactor 11 as cracking feedstock.

[0033] In the propane stripper 154, the bottom product of the ethane stripper 152 is separated, from which propylene, propane, and C4+ heavy components are isolated. A mixture of propylene and propane is collected at the top of the propane stripper 154 and fed into the propylene distillation column 155. The bottom product of the propane stripper 154 is a mixture of C4 and cracked naphtha. The mixed C4, after separation, can be sent to the MTBE synthesis unit 5, and the cracked naphtha, after separation, can be sent to the aromatics complex unit 4.

[0034] Propylene distillation column 155 is used to separate a mixture of propylene and propane into high-purity propylene (≥99.6% purity) and propane. The polymer-grade propylene collected from the top of the propylene distillation column 155 is dried by molecular sieve and then sent to the feed inlet of olefin polymer unit 2. The propane at the bottom of the column (containing trace amounts of propylene) can be recycled to the steam cracking reactor 11 as feedstock, improving the total yield of olefins, forming a closed loop of resource recycling, reducing production costs, and improving the economy and sustainability of the entire production process.

[0035] Furthermore, the hydrogenation system 41 includes: a hydrogenation refining unit 411, a hydrogen purification unit 412, a hydrogenation reforming unit 413, and an extraction unit 414; The hydrorefining unit 411 is used to hydrorefine pyrolyzed naphtha, the hydromodification unit 413 is used to hydromodify pyrolyzed light oil, the hydrogen purification unit 412 is used to separate high-purity hydrogen, and the extraction unit 414 is used to perform liquid-liquid extraction. The outlet of the hydrogen purification unit 412 is connected to the inlet of the hydrorefining unit 411 and the hydromodification unit 413. The inlet of the extraction unit 414 is connected to the outlet of the hydrorefining unit 411 and the hydromodification unit 413 through a material pipe. The outlet of the extraction unit 414 is connected to the inlet of the aromatic hydrocarbon separation system 42 through a material pipe.

[0036] In this embodiment, the hydrorefining unit 411 is used to hydrorefine pyrolyte naphtha, improving its quality through desulfurization, denitrogenation, and olefin saturation reactions to obtain C6-C8 and C9-C6 components. 10 Components.

[0037] Hydrotreating unit 413 is used to hydrotreat cracked light oil, performing desulfurization, denitrogenation, and olefin saturation reactions on the cracked light oil, retaining monocyclic aromatics, and obtaining C6-C8 components and C9-C4 components. 10 Components.

[0038] The hydrogen purification unit 412 is used to separate high-purity hydrogen from the hydrogen-rich gas and methane hydrogen in DCC unit 1, and to recycle the high-purity hydrogen back to the hydrorefining unit 411 and the hydromodification unit 413.

[0039] Extraction unit 414 is used to perform liquid-liquid extraction on the C6-C8 components of hydrorefining unit 411 and hydromodification unit 413 to obtain benzene, toluene, xylene and raffinate, which are then sent to aromatic separation system 42 through material pipeline.

[0040] Furthermore, the aromatic hydrocarbon separation system 42 includes: a heavy aromatic hydrocarbon adsorption and separation module 421 and a desorption module 422; The inlet of the desorption module 422 is connected to the outlet of the hydrorefining unit 411, the hydromodification unit 413 and the heavy aromatics adsorption and separation module 421 via a pipeline, and the outlet of the desorption module 422 is connected to the inlet of the rubber synthesis unit 7 via a material pipe.

[0041] In this embodiment, the heavy aromatic hydrocarbon adsorption and separation module 421 is used to utilize the polarity difference between aromatic and non-aromatic components and to separate C9-C4 hydrocarbons through a simulated moving bed. 10 The components were separated and purified to obtain C9 aromatics and C24 aromatics. 10 Aromatic hydrocarbons and non-aromatic solvent oils.

[0042] The desorption module 422 is used to desorb the aromatic components in the heavy aromatic adsorption and separation module 421, the hydrorefining unit 411, and the hydroreforming unit 413 to obtain high-purity aromatic products, which are then sent to the rubber synthesis unit 7 through a material pipeline. The aromatic components include benzene, toluene, xylene, C9 aromatics, and C6 aromatics. 10 Aromatic hydrocarbons.

[0043] In a preferred embodiment, specifically, the hydrorefining unit 411 is used to desulfurize and denitrogenate cracked naphtha (containing 1000-3000 ppm sulfur, 200-500 ppm nitrogen, and 20-40% olefins) to meet the requirements of extraction feed. Hydrogen is used to perform an olefin saturation reaction on the cracked naphtha, converting diolefins into alkanes to reduce polymerization coking in subsequent equipment, yielding C6-C8 components and C9-C4 components. 10 Components.

[0044] Hydrotreating unit 413 is used for selective hydrogenation of cracked light oil (containing 15-30% bi / polycyclic aromatics and 2000-5000 ppm sulfur), targeting the breaking of CS / CN bonds (preserving the aromatic ring structure) while saturating only side-chain olefins (avoiding octane number loss due to aromatic ring opening), yielding C6-C8 components (monocyclic aromatics, such as benzene, toluene, and xylene), and C9-C... 10 Components (heavy aromatic hydrocarbons, such as cumene and mesitylene).

[0045] The hydrogen purification unit 412 is used to purify hydrogen-rich gas to over 95% purity, obtaining high-purity hydrogen. Alternatively, it can perform pressure swing adsorption on methane to obtain 99.9% high-purity hydrogen. The produced hydrogen is sent to the hydrorefining unit 411 and the hydromodification unit 413, which can significantly improve the utilization rate of hydrogen and reduce the cost of replenishing new hydrogen.

[0046] Extraction unit 414 uses sulfolane and water (85:15 ratio) for liquid-liquid extraction of C6-C8 components, setting the extraction temperature to 80-100℃ to obtain benzene, toluene, xylene, and raffinate. Heavy aromatics adsorption and separation module 421 uses a simulated moving bed (exemplarily selecting 12 tower beds, switching cycle 8-12 minutes, desorbent being a toluene / para-xylene mixture) for the adsorption and separation of C9-C8 components. 10 The components were separated and purified to obtain C9 aromatics and C24 aromatics. 10 Aromatic and non-aromatic solvent oils. Furthermore, the non-aromatic solvent oil can be fed into the rubber synthesis unit 7 as a filler oil or processing oil.

[0047] Furthermore, the outlet of the extraction unit 414 is connected to the inlet of the steam cracking reactor 11 of the DCC unit 1 via a pipeline to form a closed loop.

[0048] In a preferred embodiment, the raffinate from the hydrogenation system 41 is connected via a pipeline to the inlet of the steam cracking reactor 11 in the DCC unit 1, forming a material circulation loop. This avoids the raffinate from being directly output as low-value fuel. Through reprocessing, it is converted into high-value-added chemical raw materials, reducing raw material costs and improving resource utilization. Furthermore, those skilled in the art can install pretreatment mechanisms, such as distillation columns or adsorption columns, before the raffinate enters the steam cracking reactor 11 to further purify and separate the raffinate, removing impurities and unwanted components.

[0049] Furthermore, the top outlet of the MTBE reactive distillation column 52 is connected to the feed inlet of the steam cracking reactor 11 via a pipeline, the upper outlet of the MTBE reactive distillation column 52 is connected to the inlet of the dehydrogenation reactor 61 via a pipeline, and the outlet of the dehydrogenation reactor 61 is connected to the inlet of the rubber synthesis unit 7 via a pipeline.

[0050] In this embodiment, the hydrogenation reactor 51 is used to hydrogenate the mixed C4 to obtain a purified C4 fraction, and to convert butadiene in the mixed C4 into butene and sulfur-containing compounds into hydrogen sulfide.

[0051] MTBE reactive distillation column 52 is used to etherify C4 fraction with methanol to produce MTBE, and to separate the generated MTBE. The methane distilled from the top of MTBE reactive distillation column 52 is condensed and refluxed to steam cracking reactor 11, and high-purity MTBE is obtained from the bottom of the column. The upper and middle parts of the column are enriched with MTBE etherified C4 fraction.

[0052] The dehydrogenation reactor 61 is used to dehydrogenate the MTBE post-ether C4 in the MTBE reactive distillation column 52 to produce 1,3-butadiene, which is then sent to the rubber synthesis unit 7 through a material pipeline.

[0053] In a preferred embodiment, specifically, the MTBE post-ether C4 hydrocarbons (mainly containing butene, butane, and other C4 hydrocarbons, the remaining components after MTBE synthesis) produced by the MTBE reactive distillation column 52 undergo butene / butane dehydrogenation to produce 1,3-butadiene. The dehydrogenation reaction is endothermic, therefore requiring external heating. The temperature is approximately 550-650°C, and the pressure is negative or low positive. By reducing the partial pressure, the equilibrium is shifted towards dehydrogenation. After cooling, the reaction gas is separated into 1,3-butadiene through distillation, and the byproduct hydrogen can be sent to the hydrogen purification unit 412 for reuse.

[0054] A hydrogenation reaction is performed on a mixed C4 fraction (containing butadiene, butene, butane, and sulfur-containing compounds) to convert the butadiene into butene, avoiding polymerization side reactions in the subsequent etherification reaction. The sulfur-containing compounds (such as thiols and thioethers) are converted into hydrogen sulfide for easier removal later. The purified C4 fraction, containing isobutylene, reacts with methanol to produce MTBE (methyl tert-butyl ether). The reaction products can be separated by distillation. The top of the distillation column contains light components (such as methane, ethane, and unreacted methanol vapor), which can be condensed and partially refluxed as feedstock for steam cracking reactor 11. The upper and middle sections of the column contain MTBE-etherified C4, which can be dehydrogenated in dehydrogenation reactor 61 to produce 1,3-butadiene. The bottom of the column contains high-purity MTBE (purity ≥99.5%). This stepwise utilization of the mixed C4 fraction makes the overall process more economical and environmentally friendly.

[0055] Furthermore, the styrene-butadiene rubber production line 72 includes: a styrene production unit 721, a separator 722, and a polymerization unit 723; The outlet of the styrene production unit 721 is connected to the inlet of the separator 722 via a pipe, and the outlet of the separator 722 is connected to the inlets of the styrene production unit 721 and the polymerization unit 723 via pipes.

[0056] In this embodiment, the butadiene rubber production line 71 is used to polymerize 1,3-butadiene prepared according to the butadiene preparation unit 6 to produce butadiene rubber.

[0057] In a preferred embodiment, the butadiene rubber production line 71 refines the 1,3-butadiene from the dehydrogenation reactor 61 to remove impurities (such as water, oxygen, alkynes, sulfides, etc.), and then performs directional polymerization under the action of a catalyst to generate butadiene rubber mainly composed of cis-1,4-polybutadiene.

[0058] The catalyst used can be a nickel-based, titanium-based, or cobalt-based catalyst; no specific limitation is made here, and the selection should be made by those skilled in the art based on actual needs. 1,3-Butadiene undergoes coordination anionic polymerization under the action of the catalyst to form linear polymer chains, producing cis-butadiene rubber. The reactor can be a continuous stirred tank reactor or a tubular reactor, with a reaction temperature of 50-120℃ and a pressure of 0.5-1.0 MPa. An inert solvent (such as hexane or cyclohexane) is used to dilute the butadiene, reducing the system viscosity and facilitating heat transfer and stirring.

[0059] In this embodiment, the styrene production unit 721 uses methanol as a methyl source to methylate the toluene side chain under the action of a catalyst and then dehydrogenates it to produce styrene.

[0060] Separator 722 is used to separate the liquid phase mixture and the gas phase mixture from the reaction mixture of the styrene production unit 721, and to recycle the gas phase mixture back to the styrene production unit 721. The liquid phase mixture is purified by distillation to obtain high-purity styrene, and the high-purity styrene is sent to the polymerization unit 723 through a material pipeline; Polymerization unit 723 is used to polymerize high-purity styrene with 1,3-butadiene to styrene-butadiene rubber.

[0061] In a preferred embodiment, methanol is used as the methyl source, and toluene reacts with methanol in an alkylation reaction to produce ethylbenzene under the action of an acidic catalyst. Ethylbenzene is then dehydrogenated in the action of a catalyst to produce styrene.

[0062] After cooling, the reaction mixture for preparing styrene contains hydrogen, unreacted toluene, methanol, and byproducts (such as ethylene and propylene). The gas phase mixture can be compressed and desulfurized. Toluene and methanol are recycled back to the styrene unit 721, and hydrogen can be sent to the hydrogen purification unit 412 for reuse. The liquid phase mixture contains ethylbenzene, styrene, water, and heavy components.

[0063] After removing light components such as water and methanol from the liquid mixture, vacuum distillation is performed to lower the boiling point and prevent styrene self-polymerization, yielding high-purity (≥99.6%) styrene. This high-purity styrene is then sent to polymerization unit 723 to polymerize with 1,3-butadiene to produce styrene-butadiene rubber.

[0064] Those skilled in the art can control the hardness and elasticity of styrene-butadiene rubber by adjusting the ratio of styrene to 1,3-butadiene (exemplarily, the styrene content is set to 20%-30%). Higher styrene content results in greater rubber hardness, improving wear resistance, but decreasing elasticity. The polymerization reactor is a multi-stage continuous stirred tank at a temperature of 5-10°C; low-temperature polymerization reduces branching and improves elasticity. The emulsifier for the polymerization reaction can be a fatty acid salt (such as sodium stearate) to form an oil-in-water emulsion, and the initiator can be potassium persulfate, suitable for low-temperature initiation, such as around 5°C.

[0065] Furthermore, it also includes: a copolymerization reactor 8; The inlet of the hydrogenation reactor 51 is connected to the outlet of the butadiene preparation unit 6 via a pipeline, and the inlet of the copolymerization reactor 8 is connected to the outlet of the hydrogenation reactor 51 and the polymerization-grade ethylene discharge outlet of the DCC unit 1 via pipelines.

[0066] In this embodiment, the hydrogenation reactor 51 is connected to the outlet of the butadiene preparation unit 6 and is used to carry out the hydrogenation catalytic reaction of 1,3-butadiene to generate α-olefins, which are then fed into the copolymerization reactor 8 through a material pipeline.

[0067] The copolymerization reactor 8 is connected to the discharge port of the polymer-grade ethylene in DCC unit 1, and is used to copolymerize the polymer-grade ethylene with α-olefins to generate POE polymer solution.

[0068] In a preferred embodiment, specifically, during the hydrogenation catalytic reaction of 1,3-butadiene, by controlling the degree of hydrogenation, only one double bond is reduced, while the terminal double bond is retained. The main reaction produces 1-butene (an α-olefin), and the side reaction produces butane. Subsequently, the product of the hydrogenation catalytic reaction is dehydrogenated and then distilled to remove butane and unreacted 1,3-butadiene, yielding high-purity 1-butene.

[0069] A copolymerization reaction of polymer-grade ethylene and 1-butene is achieved using metallocene catalysts or catalysts used in olefin polymerization to obtain a POE polymer solution. During the copolymerization process, those skilled in the art can select the reaction temperature, reaction pressure, and reactor based on the suitability of the catalyst used.

[0070] It should be noted that in the accompanying drawings of this utility model, the lines marked with arrows represent the connections between various components, while the lines without arrows represent the inclusion relationship between larger and smaller components.

[0071] In practical implementation, this utility model achieves full resource utilization of inferior residual oil through the technical integration and collaborative processing of various units, thereby increasing its economic value. It effectively solves the problem that existing processing methods for inferior residual oil do not fully reflect its value and have low economic benefits. Furthermore, based on the existing industry, it systematically plans the remaining products from inferior residual oil processing, determines processing and utilization pathways according to product characteristics, completes the inferior residual oil processing industrial chain, and improves enterprise economic benefits.

[0072] The above description is only a preferred embodiment of the present utility model, but the protection scope of the present utility model is not limited thereto. Any equivalent substitutions or changes made by those skilled in the art within the technical scope disclosed in the present utility model, based on the technical solution and the inventive concept of the present utility model, should be included within the protection scope of the present utility model.

Claims

1. A co-processing system for low-quality residual oil, characterized in that: include: The DCC unit (1), olefin polymer unit (2), carbon black production unit (3), aromatic hydrocarbon complex unit (4), MTBE synthesis unit (5), butadiene preparation unit (6), and rubber synthesis unit (7). The outlet of the DCC unit (1) is connected to the inlet of the olefin polymer unit (2), the carbon black production unit (3), the aromatic hydrocarbon complex unit (4), and the MTBE synthesis unit (5), respectively. The outlet of the MTBE synthesis unit (5) is connected to the inlet of the butadiene preparation unit (6), and the outlet of the butadiene preparation unit (6) is connected to the inlet of the rubber synthesis unit (7). The outlet of the aromatic hydrocarbon complex unit (4) is connected to the inlet of the rubber synthesis unit (7); The DCC unit (1) includes: a steam cracking reactor (11), a fractionation tower (12), a cracked gas compressor (13), an impurity removal device (14), and a cryogenic separation system (15). The steam cracking reactor (11), the fractionation tower (12), the cracked gas compressor (13), the impurity removal device (14), and the cryogenic separation system (15) are connected in series and configured to produce polymer-grade ethylene and polymer-grade propylene from inferior residue oil, and to produce byproducts such as hydrogen-rich gas, methane hydrogen, mixed C4, cracked naphtha, cracked light oil, and cracked heavy oil.

2. The co-processing system for inferior residual oil according to claim 1, characterized in that: The fractionation tower (12) includes: a cracked gas production outlet (121), a cracked naphtha production outlet (122), a cracked light oil discharge outlet (123), and a cracked heavy oil discharge outlet (124). The fractionation tower (12) is provided with the cracked gas outlet (121) and the cracked naphtha outlet (122) at the top of the tower, the cracked light oil outlet (123) is provided at the side of the fractionation tower (12), and the cracked heavy oil outlet (124) is provided at the bottom of the fractionation tower (12). The cracked gas outlet (121) is connected to the inlet of the cracked gas compressor (13) through a material pipe. The cracked naphtha outlet (122) and the cracked light oil outlet (123) are both connected to the feed port of the aromatics complex unit (4) through a material pipe. The pyrolysis heavy oil outlet (124) is connected to the inlet of the carbon black production unit (3) via a material pipe.

3. The co-processing system for inferior residual oil according to claim 2, characterized in that: The olefin polymer unit (2) includes a polyethylene production line (21) and a polypropylene production line (22) arranged in parallel. The feed inlet of the olefin polymer unit (2) is connected to the discharge outlets of the polymer-grade ethylene and polymer-grade propylene of the DCC unit (1) through material pipes. The carbon black production unit (3) includes a high-temperature pyrolysis reactor (31), a quench collection system (32), and a pretreatment device (33). The aromatics complex unit (4) includes a hydrogenation system (41) and an aromatics separation system (42). The feed inlet of the aromatics complex unit (4) is connected to the cracked naphtha outlet (122), cracked light oil outlet (123), methane hydrogen outlet and hydrogen-rich gas outlet of the DCC unit (1) through a material pipe. The MTBE synthesis unit (5) includes a hydrogenation reactor (51) and an MTBE reactive distillation column (52) arranged in series. The feed inlet of the MTBE synthesis unit (5) is connected to the mixed C4 outlet of the DCC unit (1) through a material pipe. The outlet of the MTBE synthesis unit (5) is connected to the inlet of the butadiene preparation unit (6) through a material pipe. The butadiene preparation unit (6) includes a dehydrogenation reactor (61), an isomerization reactor (62) and a product separation tower (63) connected in sequence. The outlet of the butadiene preparation unit (6) is connected to the inlet of the rubber synthesis unit (7) through a material pipe. The rubber synthesis unit (7) includes a butadiene rubber production line (71) and a styrene-butadiene rubber production line (72) arranged in parallel. The feed inlet of the rubber synthesis unit (7) is connected to the discharge outlet of the butadiene preparation unit (6) and the aromatic hydrocarbon combination unit (4) through a material pipe.

4. The co-processing system for inferior residual oil according to claim 1, characterized in that: The cryogenic separation system (15) includes: a demethanizer (151), a deethaner (152), an ethylene distillation column (153), a depropanizer (154), and a propylene distillation column (155). The inlet of the demethanizer (151) is connected to the outlet of the impurity removal device (14), the top of the demethanizer (151) is connected to the inlet of the aromatic hydrocarbon complex unit (4) through a pipe, and the bottom of the demethanizer (151) is connected to the inlet of the deethaner (152) through a pipe. The top of the deethanizer (152) is connected to the inlet of the ethylene distillation column (153) via a pipe, and the bottom of the deethanizer (152) is connected to the inlet of the depropaneizer (154) via a pipe; The top of the ethylene distillation column (153) is connected to the feed inlet of the olefin polymer unit (2) via a pipe, and the bottom of the ethylene distillation column (153) is connected to the inlet of the steam cracking reactor (11) via a pipe. The top of the depropanizer (154) is connected to the inlet of the propylene distillation column (155) via a pipeline, and the bottom of the depropanizer (154) is connected to the inlet of the MTBE synthesis unit (5) via a pipeline. The top of the propylene distillation column (155) is connected to the feed inlet of the olefin polymer unit (2) via a pipe, and the bottom of the propylene distillation column (155) is connected to the inlet of the steam cracking reactor (11) via a pipe.

5. The co-processing system for inferior residual oil according to claim 3, characterized in that: The hydrogenation system (41) includes: a hydrogenation refining unit (411), a hydrogen purification unit (412), a hydrogenation reforming unit (413), and an extraction unit (414). The hydrorefining unit (411) is used to hydrorefine pyrolyzed naphtha, the hydromodification unit (413) is used to hydromodify pyrolyzed light oil, the hydrogen purification unit (412) is used to separate high-purity hydrogen, and the extraction unit (414) is used to perform liquid-liquid extraction. The outlet of the hydrogen purification unit (412) is connected to the inlet of the hydrogen refining unit (411) and the hydrogen reforming unit (413). The inlet of the extraction unit (414) is connected to the outlet of the hydrogen refining unit (411) and the hydrogen reforming unit (413) through a material pipe. The outlet of the extraction unit (414) is connected to the inlet of the aromatic separation system (42) through a material pipe.

6. The co-processing system for inferior residual oil according to claim 5, characterized in that: The aromatic hydrocarbon separation system (42) includes: a heavy aromatic hydrocarbon adsorption and separation module (421) and a desorption module (422). The inlet of the desorption module (422) is connected to the outlet of the hydrorefining unit (411), the hydroreforming unit (413) and the heavy aromatic adsorption and separation module (421) via a pipeline, and the outlet of the desorption module (422) is connected to the inlet of the rubber synthesis unit (7) via a material pipe.

7. The co-processing system for inferior residual oil according to claim 5, characterized in that: The outlet of the extraction unit (414) is connected to the feed inlet of the steam cracking reactor (11) of the DCC unit (1) through a pipeline to form a closed loop.

8. The co-processing system for inferior residual oil according to claim 3, characterized in that: The top outlet of the MTBE reactive distillation column (52) is connected to the feed inlet of the steam cracking reactor (11) via a pipeline. The upper outlet of the MTBE reactive distillation column (52) is connected to the inlet of the dehydrogenation reactor (61) via a pipeline. The outlet of the dehydrogenation reactor (61) is connected to the inlet of the rubber synthesis unit (7) via a pipeline.

9. The co-processing system for inferior residual oil according to claim 3, characterized in that: The styrene-butadiene rubber production line (72) includes: a styrene production unit (721), a separator (722), and a polymerization unit (723). The outlet of the styrene production unit (721) is connected to the inlet of the separator (722) via a pipe, and the outlet of the separator (722) is connected to the inlets of the styrene production unit (721) and the polymerization unit (723) via pipes respectively.

10. The co-processing system for inferior residual oil according to claim 3, characterized in that: Also includes: Copolymer reactor (8); The inlet of the hydrogenation reactor (51) is connected to the outlet of the butadiene preparation unit (6) via a pipeline, and the inlet of the copolymerization reactor (8) is connected to the outlet of the hydrogenation reactor (51) and the polymerization-grade ethylene discharge outlet of the DCC unit (1) via pipelines.

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