Combined apparatus of atmospheric residue vacuum distillation, delayed viscosity reduction and solvent deasphalting

Abstract

The utility model relates to a kind of atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting combined device, and the combined device includes:(1) vacuum distillation heating furnace, wherein the vacuum distillation heating furnace includes feed inlet and discharge outlet;(2) vacuum distillation column, wherein the bottom discharge outlet of the vacuum distillation column is connected with the feed inlet of the vacuum distillation heating furnace by pipeline;(3) delayed viscosity reduction tank, wherein the feed inlet of the delayed viscosity reduction tank is connected with the bottom discharge outlet of the vacuum distillation column by pipeline;(4) delayed viscosity reduction flash tank, wherein the middle feed inlet of the delayed viscosity reduction flash tank is connected with the discharge outlet of the top of the delayed viscosity reduction tank by pipeline;(5) solvent deasphalting device, wherein the deasphalting device is connected with the bottom discharge outlet of the delayed viscosity reduction flash tank by pipeline.

Description

Technical Field

[0001] This utility model relates to a processing device for inferior heavy oil, specifically to a combined device for atmospheric residue oil vacuum distillation-delayed viscosity reduction-solvent deasphalting. Background Technology

[0002] The processing of heavy and low-quality crude oil is both a challenge and a potential source of profit growth in the petroleum processing industry. The combined solvent deasphalting and catalytic cracking process is the most technically and economically efficient for processing low-quality heavy oil. Improving the efficiency of this combined process has been a constant goal for refineries. East China University of Science and Technology and Beijing Research Institute of Petroleum and Chemical Technology have respectively developed a combined process of delayed viscosity reduction-solvent deasphalting-catalytic cracking for vacuum residue and a process of viscosity reduction cracking-solvent deasphalting-catalytic cracking for vacuum residue (Dr. Lu Shanxiang's dissertation: Research on Deasphalting and Demetallization of Residue Oil, East China University of Science and Technology, 1988; Research on Solvent Deasphalting of Huangdao Crude Oil Viscosity Residue, Petroleum Asphalt, 1991, No. 1, pp. 11-16). In the former, vacuum residue is drawn from the bottom of the vacuum distillation tower and enters a delayed viscosity reduction tank for a certain period of time. Then, the viscosity reduction residue enters the solvent deasphalting unit to be separated into deasphalted oil and deoiled asphalt. The deasphalted oil is used as feedstock for catalytic cracking or hydrocracking, and the deoiled asphalt can produce higher-value asphalt products. Its advantage is that it only requires adding to the delayed viscosity reduction tank, but its disadvantage is that the mild thermal cracking temperature of vacuum residue is low, making it difficult to achieve satisfactory upgrading effect. The latter process involves first heating the vacuum residue in a viscous-reducing furnace, then reacting it in a viscous-reducing reaction tower. The viscous residue is then separated into deasphalted oil and deoiled bitumen in a solvent deasphalting unit. The deasphalted oil is used as feedstock for catalytic cracking or hydrocracking. The advantage of this process is that the mild thermal cracking temperature of the vacuum residue can meet the process upgrading requirements. However, its disadvantages are that a new viscous-reducing furnace must be built, resulting in a large investment. Furthermore, the vacuum residue must be cooled before being heated to a higher reaction temperature, leading to high energy consumption and processing costs. Additionally, the deoiled bitumen, due to its high softening point, can only be used as a low-value coking feedstock or fuel.

[0003] Therefore, there is a need for a new device that can raise the mild thermal cracking temperature of vacuum residue to a suitable level without increasing investment costs and processing expenses. Utility Model Content

[0004] The purpose of this invention is to overcome the shortcomings of existing technologies. This invention provides a combined unit for atmospheric residue oil vacuum distillation-delayed viscosity reduction-solvent deasphalting, comprising:

[0005] (1) A vacuum distillation heating furnace, wherein the vacuum distillation heating furnace includes a feed inlet and a discharge outlet;

[0006] (2) A vacuum distillation column, wherein the bottom outlet of the vacuum distillation column is connected to the inlet of the vacuum distillation heater via a pipeline;

[0007] (3) Delayed viscosity reduction tank, wherein the feed inlet of the delayed viscosity reduction tank is connected to the bottom outlet of the vacuum distillation column via a pipeline;

[0008] (4) Delayed viscosity reduction flash tank, wherein the middle feed inlet of the delayed viscosity reduction flash tank is connected to the discharge outlet at the top of the delayed viscosity reduction tank via a pipeline;

[0009] (5) Solvent deasphalting device, wherein the solvent deasphalting device is connected to the bottom outlet of the delayed viscosity reduction flash tank via a pipeline.

[0010] In an embodiment of this utility model, a flow regulating valve is installed on the pipeline connecting the bottom outlet of the vacuum distillation column to the feed inlet of the vacuum distillation heater.

[0011] In an embodiment of this utility model, the top outlet of the delayed viscosity-reducing flash evaporator is connected to a fractionation device via a pipeline.

[0012] In an embodiment of this utility model, the outlet temperature of the vacuum distillation furnace is less than or equal to 410°C.

[0013] In an embodiment of this utility model, the outlet temperature of the vacuum distillation column is 375-405℃.

[0014] Compared with the prior art, the technical advantages of this utility model include:

[0015] 1. It reduces equipment investment, eliminates the need for a new anti-sticking heating furnace, and also saves the energy required for heating materials in the anti-sticking heating furnace;

[0016] 2. It meets the optimization requirements of the mild thermal cracking-solvent deasphalting combined process for increasing viscosity reduction temperature, improves the yield and quality of deasphalted oil, thereby increasing the quantity and quality of feedstock for subsequent cracking processes and thus increasing the economic benefits of refineries; moreover, deasphalted asphalt can be used as a higher-value asphalt product or blending component.

[0017] 3. Because it can increase the temperature of the vacuum residue at the bottom of the vacuum distillation tower, it can greatly reduce the reaction time of mild thermal cracking, thereby greatly reducing the volume of the delayed viscous reduction tank. This not only reduces equipment investment, but also avoids the danger of storing large amounts of high-temperature hot oil.

[0018] 4. Increasing the flow rate of the vacuum distillation heater can alleviate coking in the furnace tubes (e.g., oil transfer line) and extend the operating cycle of the unit.

[0019] Other features and aspects will become clear from the following detailed description, accompanying drawings, and claims. Attached Figure Description

[0020] The present invention can be better understood by describing exemplary embodiments of the present invention in conjunction with the accompanying drawings, in which:

[0021] Figure 1 This diagram shows a schematic of a combined atmospheric residue distillation-delayed viscosity reduction-solvent deasphalting device according to a specific embodiment of the present invention.

[0022] Among them, 1-reduced pressure distillation heating furnace; 2-reduced pressure distillation tower; 3-delayed viscosity reduction tank; 4-delayed viscosity reduction flash tank; 5-solvent deasphalting unit; 6-atmospheric residue oil feed line; 7-oil transfer line from the reduced pressure distillation heating furnace to the reduced pressure distillation tower; 8-reduced pressure residue oil extraction line; 9-reduced pressure residue oil extraction line to the reduced pressure distillation heating furnace feed line; 10-reduced pressure residue oil extraction line to the delayed viscosity reduction tank; 11-pipeline from the delayed viscosity reduction tank to the viscosity reduction flash tank; 12-pipeline from the viscosity reduction flash residue oil to the solvent deasphalting unit; 13-flash light oil pipeline; 14-flow regulating valve; a-atmospheric pressure residue oil; b-deasphalted oil; c-deoiled asphalt.

[0023] Figure 2 This diagram shows a conventional atmospheric residue vacuum distillation-viscosity reduction-solvent deasphalting combined unit in the prior art.

[0024] Among them, 21-reduced pressure distillation heater; 22-reduced pressure distillation tower; 23-thickness reduction heater; 24-thickness reduction reactor; 25-thickness reduction flash tank; 26-solvent deasphalting unit; 27-oil transfer line from reduced pressure distillation heater to reduced pressure distillation tower; 28-reduced pressure residue oil extraction line to thickening heater; 29-feed line from thickening heater to thickening reactor; 210-pipeline from thickening reactor to thickening flash tank; 211-pipeline from thickening flash tank to solvent deasphalting unit; 212-flash light oil pipeline; a-atmospheric pressure residue oil; b-deasphalted oil; c-deoiled asphalt. Detailed Implementation

[0025] Unless otherwise defined, the technical or scientific terms used in the claims and description shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention pertains.

[0026] In existing crude oil atmospheric and vacuum distillation units, the outlet temperature of the vacuum distillation heater generally cannot exceed 410℃; otherwise, coking will occur on the transfer line 7 from the vacuum distillation heater to the vacuum distillation tower. Under this limitation, the inlet material temperature of the subsequent delayed viscosity reduction tank cannot reach the ideal temperature of 375-405℃ required for vacuum residue viscosity reduction. However, by using the atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting combined unit of this invention, a portion of the vacuum residue is circulated back to the inlet of the vacuum distillation heater from the bottom outlet of the vacuum distillation tower through pipelines. Unexpectedly, this ensures that the vacuum residue temperature at the bottom outlet of the vacuum distillation tower reaches 375-405℃, 385-405℃, or 395-405℃.

[0027] like Figure 1 As shown, the atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting combined device provided by this utility model mainly includes a vacuum distillation heater 1, a vacuum distillation tower 2, a delayed viscosity reduction tank 3, a delayed viscosity reduction flash tank 4, and a solvent deasphalting device 5. Atmospheric residue a enters the vacuum distillation heater 1 through pipeline 6, and after heating, enters the vacuum distillation tower 2 through the oil transfer line 7 between the vacuum distillation heater 1 and the vacuum distillation tower 2. After vacuum distillation, the vacuum residue is extracted from the bottom of the vacuum distillation tower 2 through pipeline 8. A portion of the vacuum residue is recycled back to the vacuum distillation heater 1 through pipeline 9, and the other portion enters the delayed viscosity reduction tank 3 through pipeline 10. In some embodiments, a portion of the vacuum residue is incorporated into pipeline 6 through pipeline 9 and then enters the vacuum distillation heater 1 along with the ambient temperature residue a. In some embodiments, the amount of vacuum residue entering pipeline 9 is adjusted by a flow regulating valve 14, thereby regulating the temperature of the vacuum residue at the bottom of the vacuum distillation tower 2, i.e., the feed temperature of the delayed viscosity reduction tank 3. The delayed viscosity reduction tank 3 is connected to the delayed viscosity reduction flash tank 4 via pipeline 11. The bottom of the delayed viscosity reduction flash tank 4 is connected to the solvent deasphalting unit 5 via pipeline 12, wherein the solvent deasphalting unit 5 produces deasphalted oil b and deoiled asphalt c. Additionally, the top of the delayed viscosity reduction flash tank 4 is connected to other fractionation systems (not shown in the figure) via pipeline 13. In this invention, the setup parameters and operating conditions of each device can be referenced from conventional atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting combined units in the art, and will not be elaborated further here.

[0028] like Figure 2As shown, a conventional atmospheric residue vacuum distillation-viscosity reduction-solvent deasphalting combined unit in the prior art mainly includes a vacuum distillation heater 21, a vacuum distillation tower 22, a viscosity reduction heater 23, a viscosity reduction reactor 24, a viscosity reduction flash tank 25, and a solvent deasphalting unit 26. Atmospheric residue a enters the vacuum distillation heater 21, and after heating, enters the vacuum distillation tower 22 via the transfer line 27 between the vacuum distillation heater 21 and the vacuum distillation tower 22. After vacuum distillation, the vacuum residue oil enters the viscosity reduction heater 23 through pipeline 28 at the bottom of the vacuum distillation tower 22. Then, it enters the viscosity reduction reactor 24 through pipeline 29. Subsequently, the material enters the viscosity reduction flash tank 25 through pipeline 210. The bottom of the viscosity reduction flash tank 25 is connected to the solvent deasphalting unit 26 through pipeline 211, whereby the solvent deasphalting unit 26 produces deasphalted oil b and de-oiled asphalt c. In addition, the top of the viscosity-reducing flash tank 25 is connected to other fractionation systems (not shown in the figure) via pipeline 212.

[0029] Example

[0030] Example 1

[0031] according to Figure 1 The apparatus shown is implemented. Atmospheric residue from a certain imported crude oil enters vacuum distillation heater 1 for heating. The outlet temperature of the heater is 408℃. The temperature of the vacuum residue extracted from the bottom of vacuum distillation tower 2 is measured to be 390℃. After staying in the delayed viscosity reducing tank 3 for 2.0 hours, the delayed viscosity reducing residue enters solvent deasphalting unit 5 for separation into deasphalted oil and deoiled asphalt. The yield and composition properties of each product are listed in Table 1.

[0032] Example 2

[0033] according to Figure 1 The apparatus shown is implemented. Atmospheric residue from a certain imported crude oil enters vacuum distillation furnace 1 for heating. The outlet temperature of the furnace is 408℃. The temperature of the vacuum residue extracted from the bottom of vacuum distillation tower 2 is measured to be 380℃. After staying in the delayed viscosity reducing tank 3 for 4.5 hours, the delayed viscosity reducing residue enters solvent deasphalting unit 5 for separation into deasphalted oil and deoiled asphalt. The yield and composition properties of each product are listed in Table 1.

[0034] Example 3

[0035] according to Figure 1 The apparatus shown is implemented. Atmospheric residue from a certain imported crude oil enters vacuum distillation heater 1 for heating. The outlet temperature of the heater is 410℃. The temperature of the vacuum residue extracted from the bottom of vacuum distillation tower 2 is measured to be 400℃. After staying in the delayed viscosity reducing tank for 1.0 hour, the delayed viscosity reducing residue enters solvent deasphalting unit 5 for separation into deasphalted oil and deoiled asphalt. The yield and composition properties of each product are listed in Table 1.

[0036] Comparative Example 1

[0037] according to Figure 1 The apparatus shown is implemented, but pipeline 9 is removed. Atmospheric residue from a certain imported crude oil enters vacuum distillation heater 1 for heating. The outlet temperature of the heater is 408℃. The temperature of the vacuum residue extracted from the bottom of vacuum distillation tower 2 is measured to be 370℃. After staying in the delayed viscosity reducing tank for 3.0 hours, the delayed viscosity reducing residue enters solvent deasphalting unit 5 for separation into deasphalted oil and deoiled asphalt. The yield and composition properties of each product are listed in Table 1.

[0038] Comparative Example 2

[0039] According to the conventional vacuum distillation-solvent deasphalting process, i.e. Figure 1 The apparatus shown is implemented, but pipeline 9, delayed viscosity reduction tank 3, and delayed viscosity reduction flash tank 4 are omitted. Atmospheric residue from a certain imported crude oil enters vacuum distillation heater 1 for heating, with an outlet temperature of 408°C. The vacuum residue from the bottom of vacuum distillation tower 2 enters solvent deasphalting unit 5 for separation into deasphalted oil and deoiled bitumen. The yield and composition of each product are listed in Table 1.

[0040] Comparative Example 3

[0041] according to Figure 2 The conventional vacuum distillation-viscosity reduction-solvent deasphalting process flow shown is implemented. Atmospheric residue from a certain imported crude oil enters the vacuum distillation heater 21 for heating, with an outlet temperature of 408℃. The vacuum residue from the bottom of the vacuum distillation tower 22 is heated to 420℃ in the viscosity reduction heater 23 and viscosified in the viscosity reduction reactor 24 for 1.0 hour. The viscosified residue then enters the solvent deasphalting unit 26 for separation into deasphalted oil and deoiled bitumen. The yield and composition properties of each product are listed in Table 1.

[0042] Although the present invention has been described in conjunction with specific embodiments, those skilled in the art will understand that many modifications and variations can be made to the present invention. Therefore, it is to be appreciated that the claims are intended to cover all such modifications and variations that are true to the concept and scope of the present invention.

[0043] Table 1

[0044]

Claims

1. A combined unit for atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting, comprising: (1) A vacuum distillation heating furnace, wherein the vacuum distillation heating furnace includes a feed inlet and a discharge outlet; (2) A vacuum distillation column, wherein the bottom outlet of the vacuum distillation column is connected to the inlet of the vacuum distillation heater via a pipeline; (3) Delayed viscosity reduction tank, wherein the feed inlet of the delayed viscosity reduction tank is connected to the bottom outlet of the vacuum distillation column via a pipeline; (4) Delayed viscosity reduction flash tank, wherein the middle feed inlet of the delayed viscosity reduction flash tank is connected to the discharge outlet at the top of the delayed viscosity reduction tank via a pipeline; (5) Solvent deasphalting device, wherein the solvent deasphalting device is connected to the bottom outlet of the delayed viscosity reduction flash tank via a pipeline.

2. The combined atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting unit according to claim 1, wherein, A flow regulating valve is installed on the pipeline connecting the bottom outlet of the vacuum distillation column to the inlet of the vacuum distillation heater.

3. The combined atmospheric residue vacuum distillation-delayed viscosity reduction-solvent deasphalting unit according to claim 1, wherein, The top outlet of the delayed viscosity-reducing flash evaporator is connected to the fractionation unit via a pipeline.

Images