Olefin saturation system for pentane oil

Through hydrogen hydrorefining and gas, oil and liquid separation technology in pentane oil olefin saturation system, the olefin content in reformed pentane oil is reduced, the quality problem of ethylene raw materials is solved, the process flow is simplified and the coking risk is reduced. Provides high-quality ethylene raw materials.

CN222250602UActive Publication Date: 2024-12-27HENGLI PETROCHEMICAL (DALIAN) REFINING & CHEM CO LTD
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Patent Information

Application Number
CN202420133992.4
Authority / Receiving Office
CN · China
Patent Type
Utility models(China)
Current Assignee / Owner
Filing Date
2024-01-19
Publication Date
2024-12-27
Estimated Expiration
2034-01-19

AI Technical Summary

Technical Problem

The high olefin content in reformed pentane oil leads to a shortening of the operating cycle of the ethylene cracking furnace and serious coking, and there is a risk of stringing. It is necessary to reduce the olefin content to improve the quality of ethylene raw materials.

Method used

A pentane oil olefin saturation system is designed, including a pre-hydrogenation reactor, stripping tower and fractionation tower. Through hydrogen hydrogenation purification and three-phase separation technology of gas, oil and liquid, the content of olefins is reduced, and olefin saturation is achieved, and air cooling is used. The device cools the gas components and controls the quality of light naphtha.

Benefits of technology

The olefin content of pentane oil has been effectively reduced from 2-3%wt to below 0.1%wt, solving the problem of high olefin content, providing high-quality ethylene raw materials, simplifying the process flow, and reducing coking risks.

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Abstract

The utility model belongs to the technical field of reforming pentane oil olefin saturation, and particularly relates to a pentane oil olefin saturation system which comprises a pre-hydrogenation reactor, the top of the pre-hydrogenation reactor is connected through a hydrogen pipeline, the hydrogen pipeline is provided with a pre-hydrogenation raw material pipeline, and the pre-hydrogenation raw material pipeline is connected with a pentane oil inlet pipeline; the bottom of the pre-hydrogenation reactor is connected to a high-low separation process through a pipeline, a pipeline led out of the high-low separation process is connected to a stripping tower, the bottom of the stripping tower is connected with a fractionating tower through a pipeline, the fractionating tower is connected to an external tank area through a pipeline, and the bottom of the fractionating tower is connected with a reforming material pipeline; and air cooling pipelines are respectively arranged at the tops of the stripping tower and the fractionating tower. According to the utility model, the pentane oil olefin saturation process flow is simplified, the pentane oil processing flow is changed, the pentane oil is blended into the pre-hydrogenation device to be used as a raw material, and the olefin saturation function is realized by utilizing the pre-hydrofining condition; the olefin content of the pentane oil is reduced from 2-3% wt to 0.1% wt or less, and the problem of the olefin content is effectively solved.
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Description

Technical Field

[0001] The utility model belongs to the technical field of reforming pentane oil olefin saturation, and specifically relates to a pentane oil olefin saturation system. Background Art

[0002] Reformed pentane oil is an ethylene raw material. Due to its high olefin content, the olefin content of reformed pentane oil is 2-3%wt. It needs to be blended with other low-olefin ethylene materials as an ethylene raw material, or directly used as a gasoline blending component.

[0003] Since the olefin content of reformed pentane oil is 2-3%wt, the operation cycle of the ethylene cracking furnace is shortened when it is used as ethylene raw material, and coking is serious. At the same time, there is a corresponding risk of cross-contamination during the production process. Olefin saturation is required to solve the olefin content problem of pentane oil. Utility Model Content

[0004] The utility model provides a pentane oil olefin saturation system to solve the problem of high olefin content. The system can reduce the olefin content of pentane oil from 2-3%wt to below 0.1%wt, effectively solving the problem of olefin content and can be used as high-quality ethylene raw material.

[0005] In order to achieve the above-mentioned purpose, the technical scheme adopted by the utility model is: a system for saturation of olefins in pentane oil, comprising: a pre-hydrogenation reactor, the top of the pre-hydrogenation reactor is connected by a hydrogen pipeline, the hydrogen pipeline is also provided with a pre-hydrogenation raw material pipeline, the pre-hydrogenation raw material pipeline is connected to the pentane oil inlet pipeline; the bottom of the pre-hydrogenation reactor is connected to the high-low separation process by a pipeline, the pipeline leading out of the high-low separation process is connected to the stripping tower, the bottom of the stripping tower is connected to the fractionation tower by a pipeline, the fractionation tower is connected to the external tank area by a pipeline, and the bottom of the fractionation tower is connected to the reforming material pipeline; the tops of the stripping tower and the fractionation tower are respectively provided with air cooling pipelines;

[0006] Furthermore, the pentane oil in the pre-hydrogenation reactor is blended into the pre-hydrogenation unit feedstock, and the blending ratio of reformed pentane oil is 10-20% by mass on the basis of the original feed amount and ratio of the pre-hydrogenation unit remaining unchanged;

[0007] Furthermore, the high-low separation process adopts a separator for gas, oil and liquid three-phase separation; the type of separator selected is a horizontal cold low-pressure separator;

[0008] Further, the air cooling pipeline of the stripping tower is used to cool the gas at the top of the stripping tower, including: an air cooler, the inlet end of the air cooler is connected to the top of the stripping tower through a pipeline, and the outlet end of the air cooler is connected to the gas pipeline arranged on the side wall of the top of the stripping tower through a pipeline;

[0009] Furthermore, the gas pipeline is bidirectionally arranged, the air cooler outlet pipeline is connected to the gas pipeline through a tee, one end of the gas pipeline faces outside the system, and the other end is returned and connected to the stripping tower; under normal circumstances, a part of the gas in the stripping tower is discharged to the outside after being cooled by the air cooler, and a part is returned to the stripping tower, and the amount returned to the stripping tower is controlled according to the exhaust gas composition or the stripping tower pressure;

[0010] Further, the air cooling pipeline of the distillation tower is used to cool the gas at the top of the distillation tower, including: an air cooler, the inlet end of the air cooler is connected to the top of the distillation tower through a pipeline, and the outlet end of the air cooler is connected to the gas pipeline A arranged on the side wall of the top of the distillation tower through a pipeline;

[0011] Similarly, the gas pipeline A connected to the outlet end of the air cooler in the air cooling pipeline of the distillation tower is bidirectionally arranged, and the outlet pipeline of the air cooler is connected to the gas pipeline A through a tee, one end of the gas pipeline A faces outside the system, and the other end returns to the distillation tower; after cooling, part of the gas is discharged to the external tank area, and part of it flows back to the distillation tower, and the flow rate flowing back to the distillation tower is used to control the quality indicators of light naphtha and control the composition of light naphtha.

[0012] Further, the pressure of the pre-hydrogenation reactor is 2.6MPa-2.9MPa, and the reaction temperature is 290°C-305°C;

[0013] Further, the pre-hydrogenation stripping tower pressure is 0.85MPa-0.95MPa, the tower top temperature is 75°C-85°C, and the tower bottom temperature is 170°C-180°C;

[0014] Furthermore, the pre-hydrogenation fractionation tower pressure is 0.1MPa-0.15MPa, the tower top temperature is 65°C-75°C, and the tower bottom temperature is 130°C-150°C.

[0015] The process of adopting the above technical solution is:

[0016] The reformed pentane oil enters the pentane oil pipeline and is mixed with the pre-hydrogenation raw material and enters the feed buffer tank. After being heated in the heating furnace, it enters the pre-hydrogenation reactor for refining, the reformed pentane oil undergoes olefin saturation, and the hydrogenation raw material undergoes refining reactions such as desulfurization and denitrogenation. Then, after high and low fraction separation, the reaction product enters the stripping tower for stripping, and then enters the distillation tower for fractionation. The gas components after the stripping reaction are cooled by the air cooler at the top of the stripping tower and then discharged to the outside of the system. The top of the distillation tower is air-cooled and sent to the tank area as a light naphtha product. The reformed material in the distillation tower is discharged through the reforming material pipeline at the bottom of the tower.

[0017] The main purpose of this system is the reforming pre-hydrogenation unit to process atmospheric and vacuum naphtha mainly for desulfurization, denitrification and trace metal components to meet the needs of reforming processing.

[0018] The beneficial effects of adopting the technical solution of the utility model are:

[0019] The utility model simplifies the olefin saturation process of pentane oil, changes the processing process of pentane oil to blend it into a pre-hydrogenation device as a raw material, and uses pre-hydrogenation refining conditions to achieve the olefin saturation function; the olefin content of pentane oil is reduced from 2-3%wt to less than 0.1%wt, effectively solving the problem of olefin content, and can be used as a high-quality ethylene raw material. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 It is a structural schematic diagram of the utility model.

[0021] In the figure, 1, pre-hydrogenation reactor, 2, hydrogen pipeline, 3, pre-hydrogenation raw material pipeline, 4, pentane oil inlet pipeline, 5, high and low separation, 6, stripping tower, 7, distillation tower, 8, reforming material pipeline, 9, air cooler, 10, gas pipeline, 11, gas pipeline A. DETAILED DESCRIPTION

[0022] In order to make the above-mentioned purposes, features and advantages of the utility model more obvious and easy to understand, the specific implementation methods of the utility model are described in detail below in conjunction with the accompanying drawings. In the following description, many specific details are set forth to facilitate a full understanding of the utility model. However, the utility model can be implemented in many other ways different from those described herein, and those skilled in the art can make similar improvements without violating the connotation of the utility model, so the utility model is not limited by the specific embodiments disclosed below.

[0023] like Figure 1 A system for olefin saturation of pentane oil is shown, comprising: a pre-hydrogenation reactor 1, the top of the pre-hydrogenation reactor 1 is connected via a hydrogen pipeline 2, the hydrogen pipeline 2 is also provided with a pre-hydrogenation raw material pipeline 3, the pre-hydrogenation raw material pipeline 3 is connected to a pentane oil inlet pipeline 4; the bottom of the pre-hydrogenation reactor 1 is connected to a high-low separation 5 process via a pipeline, the pipeline leading out of the high-low separation 5 process is connected to a stripping tower 6, the bottom of the stripping tower 6 is connected to a fractionation tower 7 via a pipeline, the fractionation tower 7 is connected to an external tank area via a pipeline, and the bottom of the fractionation tower 7 is connected to a reforming material pipeline 8; the tops of the stripping tower 6 and the fractionation tower 7 are respectively provided with air cooling pipelines;

[0024] The pentane oil in the pre-hydrogenation reactor 1 is blended into the pre-hydrogenation unit feedstock. On the basis of the original feed amount and proportion of the pre-hydrogenation unit remaining unchanged, the blending reformed pentane oil mass ratio is 10-20% to prevent the pre-hydrogenation unit reaction pump from gasification.

[0025] The high-low separation 5 process adopts a separator for gas, oil and liquid three-phase separation; the type of separator selected is a horizontal cold low-pressure separator;

[0026] The air cooling pipeline of the stripping tower 6 is used to cool the gas at the top of the stripping tower 6, and includes: an air cooler 9, the inlet end of the air cooler 9 is connected to the top of the stripping tower 6 through a pipeline, and the outlet end of the air cooler 9 is connected to the gas pipeline 10 arranged on the top side wall of the stripping tower 6 through a pipeline; wherein the model of the air cooler 9 is A4201 AF;

[0027] The gas pipeline 10 is bidirectionally arranged, and the outlet pipeline of the air cooler 9 is connected to the gas pipeline 10 through a tee, one end of the gas pipeline 10 faces the outside of the system, and the other end returns to the stripping tower 6;

[0028] The air cooling pipeline of the distillation tower 7 is used to cool the gas at the top of the distillation tower, and includes: an air cooler 9, the inlet end of the air cooler 9 is connected to the top of the distillation tower 7 through a pipeline, and the outlet end of the air cooler 9 is connected to the gas pipeline A11 arranged on the top side wall of the distillation tower 7 through a pipeline; wherein the model of the air cooler 9 is A4301 AF;

[0029] Similarly, the gas pipeline A connected to the outlet end of the air cooler 9 in the air cooling pipeline of the distillation tower 7 is set in a bidirectional manner. The outlet pipeline of the air cooler 9 is connected to the gas pipeline A11 through a tee. One end of the gas pipeline A11 faces outside the system, and the other end returns to the distillation tower 7.

[0030] The pressure of the pre-hydrogenation reactor 1 is 2.6MPa-2.9MPa, and the reaction temperature is 290℃-305℃;

[0031] The pressure of the pre-hydrogenation stripping tower 6 is 0.85MPa-0.95MPa, the top temperature is 75℃-85℃, and the bottom temperature is 170℃-180℃;

[0032] The pressure of the pre-hydrogenation fractionation tower 7 is 0.1MPa-0.15MPa, the top temperature is 65°C-75°C, and the bottom temperature is 130°C-150°C.

[0033] The process of adopting the above technical solution is:

[0034] The reformed pentane oil enters the pentane oil pipeline 4 and is mixed with the pre-hydrogenation raw material to enter the feed buffer tank, and after being heated in the heating furnace, it enters the pre-hydrogenation reactor 1 for refining, the reformed pentane oil is olefin saturated, and the hydrogenation raw material is subjected to refining reactions such as desulfurization and denitrogenation; then after separation by high and low fractionation 5, the reaction product enters the stripping tower 6 for stripping, and then enters the fractionation tower 7 for fractionation; the gas components after the stripping reaction are cooled by the air cooler 9 at the top of the stripping tower 6 and then discharged to the outside of the system; the top of the fractionation tower 7 is air-cooled and then sent to the tank area as a light naphtha product; the reforming material in the fractionation tower 7 is discharged through the reforming material pipeline 8 at the bottom of the tower; using the above system, the olefin content of the reformed pentane oil is reduced from 2-3%wt to less than 0.1%wt.

[0035] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0036] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present utility model, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0037] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0038] In the present utility model, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediate medium. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0039] It should be noted that when an element is referred to as being "fixed to" or "disposed on" another element, it may be directly on the other element or there may be a central element. When an element is considered to be "connected to" another element, it may be directly connected to the other element or there may be a central element at the same time. The terms "vertical", "horizontal", "upper", "lower", "left", "right" and similar expressions used herein are for illustrative purposes only and do not represent the only implementation method.

Claims

1. A system for saturation of pentane oil with olefins, characterized in that: include: A pre-hydrogenation reactor, wherein the top of the pre-hydrogenation reactor is connected via a hydrogen pipeline, a pre-hydrogenation raw material pipeline is also provided on the hydrogen pipeline, and the pre-hydrogenation raw material pipeline is connected to a pentane oil inlet pipeline; the bottom of the pre-hydrogenation reactor is connected to a high-low separation process via a pipeline, and a pipeline leading out of the high-low separation process is connected to a stripping tower, the bottom of the stripping tower is connected to a fractionation tower via a pipeline, the fractionation tower is connected to an external tank area via a pipeline, and a reforming material pipeline is connected to the bottom of the fractionation tower; the tops of the stripping tower and the fractionation tower are respectively provided with air cooling pipelines.

2. A system for saturation of pentane oil with olefins according to claim 1, characterized in that: The high-low separation process adopts a separator for gas, oil and liquid three-phase separation; the type of separator selected is a horizontal cold low-pressure separator.

3. A system for saturation of pentane oil with olefins according to claim 1, characterized in that: The air cooling pipeline of the stripping tower comprises an air cooler, the inlet end of the air cooler is connected to the top of the stripping tower through a pipeline, and the outlet end of the air cooler is connected to a gas pipeline arranged on the side wall of the top of the stripping tower through a pipeline.

4. A system for saturation of pentane oil with olefins according to claim 3, characterized in that: The gas pipeline is bidirectionally arranged, and the air cooler outlet pipeline is connected to the gas pipeline through a tee, one end of the gas pipeline faces outside the system, and the other end returns and is connected to the stripping tower.

5. A system for saturation of pentane oil with olefins according to claim 1, characterized in that: The air cooling pipeline of the distillation tower comprises: an air cooler, the inlet end of the air cooler is connected to the top of the distillation tower through a pipeline, and the outlet end of the air cooler is connected to the gas pipeline A arranged on the side wall of the top of the distillation tower through a pipeline.

6. A system for saturation of pentane oil with olefins according to claim 5, characterized in that: The gas pipeline A connected to the outlet end of the air cooler in the air cooling pipeline of the distillation tower is bidirectionally set. The outlet pipeline of the air cooler is connected to the gas pipeline A through a tee. One end of the gas pipeline A faces outside the system, and the other end returns to the distillation tower.

7. A system for saturation of pentane oil with olefins according to claim 1, characterized in that: The pressure of the pre-hydrogenation reactor is 2.6MPa-2.9MPa, and the reaction temperature is 290℃-305℃.

8. A system for saturation of pentane oil with olefins according to claim 1, characterized in that: The pressure of the pre-hydrogenation stripping tower is 0.85MPa-0.95MPa, the top temperature is 75℃-85℃, and the bottom temperature is 170℃-180℃.

9. A system for saturation of pentane oil with olefins according to claim 1, characterized in that: The pressure of the pre-hydrogenation fractionation tower is 0.1MPa-0.15MPa, the top temperature is 65℃-75℃, and the bottom temperature is 130℃-150℃.