Naphtha hydrogenation system capable of switching processing flow
By designing a switchable naphtha hydrogenation system and combining valve control to achieve 'full hydrogenation' and 'pre-fractionation' mode switching, it solves the problem that chemical raw material production and refined heavy naphtha production in the existing technology are not allowed to take into account. Improves device processing adaptability and production efficiency.
Patent Information
- Application Number
- CN202420124311.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-01-18
- Publication Date
- 2024-12-27
- Estimated Expiration
- 2034-01-18
AI Technical Summary
The prior art lacks naphtha hydrogenation system that can take into account both the production of chemical raw materials and the production of refined heavy naphtha, and cannot increase the processing volume without increasing the load of the reaction system.
A naphtha hydrogenation system with switchable processing processes is designed, including feed main pipeline, pre-fractionation tower, raw material tank, heating furnace, reactor, gas-liquid separator, stripping tower and fractionation tower, controlled by valves The switching between 'full hydrogenation' and 'prefractionation' modes is achieved, and the flow rate entering the prefractionation column can be adjusted.
The switching between the two modes of "full hydrogenation" and "pre-fractionation" has been achieved, which improves the processing adaptability of the device, and can flexibly adjust the flow rate of the pre-fractionation tower to meet the needs of chemical raw materials production and refined heavy naphtha production.
Smart Images
Figure CN222250607U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of naphtha hydrogenation process, in particular to a naphtha hydrogenation system capable of switching processing flows. Background Art
[0002] Naphtha hydrogenation is the core part of the pretreatment of reforming raw materials, and its function is to remove impurities to protect the reforming catalyst. In the prior art, naphtha hydrogenation usually adopts a full-fraction hydrogenation process or a pre-fractionation process. The refined heavy naphtha produced by the two processes can meet the feed requirements of the reforming unit. Among them, the light naphtha produced by the full hydrogenation process has a low impurity content and can be used as a chemical raw material, but the load of the reaction system is relatively high; the pre-fractionation process can increase the processing capacity of the device and produce more refined heavy naphtha under the condition that the load of the reaction system remains unchanged, but the impurity content of the light naphtha at the top of the pre-fractionation tower is relatively high, which is not suitable as a chemical raw material. The prior art lacks a naphtha hydrogenation system that can take into account both the production of chemical raw materials and the production of refined heavy naphtha. Utility Model Content
[0003] In view of the defects of the prior art, the utility model provides a naphtha hydrogenation system with switchable processing flow, which can realize the switching of "full hydrogenation" and "pre-fractionation" modes, and can adjust the flow entering the pre-fractionation tower, thereby improving the processing adaptability of the device.
[0004] In order to achieve the above-mentioned purpose, the technical solution provided by the utility model is a naphtha hydrogenation system with switchable processing flow, which includes a main feed pipeline, a pre-fractionation tower, a raw material tank, a pre-fractionation discharge pipeline, a heating furnace, a reactor, a gas-liquid separator, a stripping tower and a fractionation tower; the main feed pipeline is respectively connected to the first branch feed pipeline and the second branch feed pipeline; the pre-fractionation tower is connected to the first branch feed pipeline, and the first branch feed pipeline is provided with a first valve; the raw material tank is connected to the second branch feed pipeline, and the second branch feed pipeline is provided with a first valve; two valves; a pre-fractionation discharge pipeline is connected to the bottom of the pre-fractionation tower, the pre-fractionation discharge pipeline is connected to the second branch feed pipeline, and the meeting point with the second branch feed pipeline is downstream of the second valve, and a third valve is arranged on the pre-fractionation discharge pipeline; a heating furnace is connected to the raw material tank; a reactor is connected to the heating furnace, and a catalyst is accommodated inside the reactor; a gas-liquid separator is connected to the reactor; a stripping tower is connected to the gas-liquid separator; a distillation tower is connected to the stripping tower, and the distillation tower is connected to a refined naphtha discharge pipeline.
[0005] Furthermore, the second valve is configured as a flow regulating valve.
[0006] Furthermore, a raw material pump is provided between the raw material tank and the heating furnace.
[0007] Furthermore, the stripping tower is connected to an acid gas discharge pipeline.
[0008] Furthermore, the top of the pre-fractionation tower is connected to a light naphtha discharge pipeline.
[0009] Furthermore, a second type of light naphtha discharge pipeline is connected to the top of the distillation tower.
[0010] Furthermore, the feed temperature of the pre-fractionation tower is 90-120°C, the top pressure is 0.08-0.15MpaG, and the bottom temperature is 135-140°C.
[0011] Furthermore, the feed rate of the reactor is 400-600 t / h, the reaction temperature is 280-330° C., the space velocity is 5.5 / h, and the reaction pressure is 2.7-3.0 MpaG.
[0012] Furthermore, the feed temperature of the stripping tower is 150-158°C, the top pressure is 0.8-0.83MpaG, and the bottom temperature is 185-190°C.
[0013] Furthermore, the feed temperature of the distillation tower is 120-130°C, the top pressure is 0.08-0.15MpaG, and the bottom temperature is 140-150°C.
[0014] Further description of the utility model: it has a full hydrogenation mode and a pre-fractionation mode; when the second valve is opened, the first valve and the third valve are closed, so as to be in the full hydrogenation mode, the raw material directly enters the raw material tank, enters the heating furnace to be heated to 299-301°C, passes through a reactor equipped with a catalyst, and the reaction product is separated by a subsequent gas-liquid separator, a stripping tower, and a fractionation tower, and the acid gas, light naphtha and the refined heavy naphtha at the bottom of the tower are respectively sent to the downstream; when the first valve and the third valve are opened, the second valve is closed, so as to be in the pre-fractionation mode, all the raw materials enter the pre-fractionation tower, the light naphtha at the top of the tower is sent to the tank area, the heavy naphtha at the bottom of the tower enters the raw material tank, enters the heating furnace to be heated to 303-305°C, passes through a reactor equipped with a catalyst, and the reaction product is separated by a subsequent gas-liquid separator, a stripping tower, and a fractionation tower, and the acid gas, light naphtha and the refined heavy naphtha at the bottom of the tower are respectively sent to the downstream.
[0015] The beneficial effects of the utility model include: the switching between the two modes of "full hydrogenation" and "pre-fractionation" can be realized, the flow rate entering the pre-fractionation tower can be flexibly adjusted, and the processing adaptability of the device is improved. BRIEF DESCRIPTION OF THE DRAWINGS
[0016] Figure 1 This is a process flow chart of a naphtha hydrogenation system with switchable processing flow in one embodiment of the utility model;
[0017] In the figure:
[0018] 100, main feed pipeline, 110, first branch feed pipeline, 111, first valve, 120, second branch feed pipeline, 121, second valve,
[0019] 200, pre-fractionator, 210, class I light naphtha discharge pipeline,
[0020] 300, raw material tank, 310, raw material pump,
[0021] 400, pre-fractionation discharge pipeline, 410, third valve,
[0022] 500. Heating furnace,
[0023] 600, reactor,
[0024] 700, gas-liquid separator,
[0025] 800, stripping tower, 810, acid gas discharge pipeline,
[0026] 900, distillation tower, 910, refined naphtha discharge pipeline, 920, Class II light naphtha discharge pipeline. DETAILED DESCRIPTION
[0027] 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.
[0028] See also Figure 1, shows a naphtha hydrogenation system with switchable processing flow in one embodiment of the utility model, which includes a main feed pipeline 100, a pre-fractionation tower 200, a raw material tank 300, a pre-fractionation discharge pipeline 400, a heating furnace 500, a reactor 600, a gas-liquid separator 700, a stripping tower 800 and a fractionation tower 900. The main feed pipeline 100 is connected to the first branch feed pipeline 110 and the second branch feed pipeline 120 respectively; the pre-fractionation tower 200 is connected to the first branch feed pipeline 110, and the first branch feed pipeline 110 is provided with a first valve 111; the raw material tank 300 is connected to the second branch feed pipeline 120, and the second branch feed pipeline 120 is provided with a second valve 121; the pre-fractionation discharge pipeline 400 is connected to the bottom of the pre-fractionation tower 200, and the pre-fractionation discharge pipeline 400 is connected to the second branch feed pipeline 120. , and the meeting point with the second branch feed pipeline 120 is downstream of the second valve 121, and a third valve 410 is provided on the pre-fractionation discharge pipeline 400; the heating furnace 500 is connected to the raw material tank 300; the reactor 600 is connected to the heating furnace 500, and a catalyst is accommodated inside the reactor 600; the gas-liquid separator 700 is connected to the reactor 600; the stripping tower 800 is connected to the gas-liquid separator 700; the distillation tower 900 is connected to the stripping tower 800, and the distillation tower 900 is connected to a refined naphtha discharge pipeline 910.
[0029] Preferably, in the specific setting, the second valve 121 is set as a flow regulating valve, which can adjust the flow entering the pre-fractionation tower 200 to control the raw materials to enter the pre-fractionation tower 200 in whole or in part. Based on this embodiment, the first valve 111 and the third valve 410 can also be set as flow regulating valves to control the process more flexibly.
[0030] The naphtha hydrogenation system with switchable processing flow has a full hydrogenation mode and a pre-fractionation mode; when the second valve 121 is opened, the first valve 111 and the third valve 410 are closed, so as to be in the full hydrogenation mode, the raw material directly enters the raw material tank 300, enters the heating furnace 500 to be heated to 299-301°C, passes through the reactor 600 equipped with a catalyst, and the reaction products are separated by the subsequent gas-liquid separator 700, the stripping tower 800, and the fractionation tower 900, and the acid gas, light naphtha and the bottom refined heavy naphtha are respectively sent to the downstream When the first valve 111 and the third valve 410 are opened, and the second valve 121 is closed, the system is in pre-fractionation mode, and all raw materials enter the pre-fractionation tower 200, the light naphtha at the top of the tower is sent to the tank area, and the heavy naphtha at the bottom of the tower enters the raw material tank 300, enters the heating furnace 500 and is heated to 303-305°C, and passes through the reactor 600 equipped with a catalyst. The reaction products are separated by the subsequent gas-liquid separator 700, the stripping tower 800, and the fractionation tower 900, and the acid gas, light naphtha and the refined heavy naphtha at the bottom of the tower are respectively sent to the downstream.
[0031] It should be noted that in the "full hydrogenation" mode, the naphtha hydrogenation feedstock directly enters the feedstock buffer tank; in the "pre-fractionation" mode, the naphtha hydrogenation feedstock first enters the pre-fractionation tower 200, the light naphtha at the top of the tower is sent to the downstream, and the heavy naphtha at the bottom of the tower enters the feedstock tank 300. The feedstock is extracted from the bottom of the feedstock tank 300, and after being pressurized by the feedstock pump, it enters the heating furnace 500 for heating. After heating, it passes through the reactor 600 equipped with a catalyst, that is, the hydrogenation reactor, and the reaction product enters the fractionation system. The separated acid gas, light naphtha and refined heavy naphtha are respectively sent to the downstream. During the production process, the "full hydrogenation" mode or the "pre-fractionation" mode can be selected according to the downstream production needs; when the "full hydrogenation" mode is adopted, the pre-fractionation tower 200 is not used, and all the feed enters the reactor 600, which increases the load of the reactor 600, and the hydrogenation product has a low impurity content and can be shipped as a high-quality product; when the "pre-fractionation" mode is adopted, the pre-fractionation tower 200 is used, and light naphtha is separated at the top of the tower, which effectively reduces the load of the hydrogenation reaction system and can process more heavy naphtha to meet the needs of the reforming unit.
[0032] The above-mentioned naphtha hydrogenation system with switchable processing flow retains the original design of the "full hydrogenation" process flow and adds a pre-fractionation tower system. The light naphtha at the top of the pre-fractionation tower is sent out, and the heavy naphtha at the bottom of the tower is heated by a heating furnace and enters the hydrogenation reactor. The reaction products are separated into light naphtha and refined heavy naphtha through subsequent product separators, stripping towers, and distillation towers for export, thereby improving the processing adaptability of the device.
[0033] In one embodiment, a raw material pump 310 is provided between the raw material tank 300 and the heating furnace 500 to increase the pressure of the raw material flowing out of the bottom of the raw material tank 300 so as to be transported to the heating furnace 500 downstream.
[0034] In one embodiment, the stripping tower 800 is connected to an acid gas discharge pipeline 810 .
[0035] In one embodiment, a light naphtha outlet pipeline 210 is connected to the top of the pre-fractionation tower 200 .
[0036] In one embodiment, a Type II light naphtha outlet pipeline 920 is connected to the top of the fractionation tower 900 .
[0037] In one embodiment, the feed temperature of the pre-fractionation tower 200 is 90-120°C, the top pressure is 0.08-0.15 MPaG, and the bottom temperature is 135-140°C.
[0038] In one embodiment, the feed rate of the reactor 600 is 400-600 t / h, the reaction temperature is 280-330° C., the space velocity is 5.5 / h, and the reaction pressure is 2.7-3.0 MpaG.
[0039] In one embodiment, the feed temperature of the stripping tower 800 is 150-158°C, the top pressure is 0.8-0.83 MPaG, and the bottom temperature is 185-190°C.
[0040] In one embodiment, the feed temperature of the distillation tower 900 is 120-130°C, the top pressure is 0.08-0.15 MPaG, and the bottom temperature is 140-150°C.
[0041] 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.
[0042] 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.
[0043] 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.
[0044] In the present utility model, unless otherwise clearly specified and limited, the first feature "above" or "below" the second feature may be 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, the first feature "above", "above" and "above" the second feature may be that the first feature is directly above or obliquely above the second feature, or simply indicates that the first feature is higher in level than the second feature. The first feature "below", "below" and "below" the second feature may be that the first feature is directly below or obliquely below the second feature, or simply indicates that the first feature is lower in level than the second feature. It should be noted that when an element is referred to as "fixed to" or "set 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", "up", "down", "left", "right" and similar expressions used herein are for illustrative purposes only and do not represent the only implementation method.
Claims
1. A naphtha hydrogenation system with switchable processing flow, characterized in that: include The main feed pipeline is connected to the first branch feed pipeline and the second branch feed pipeline respectively; a pre-fractionation tower connected to the first branch feed pipeline, wherein the first branch feed pipeline is provided with a first valve; a raw material tank connected to the second branch feed pipeline, wherein the second branch feed pipeline is provided with a second valve; a pre-fractionation discharge pipeline connected to the bottom of the pre-fractionation tower, the pre-fractionation discharge pipeline connected to the second branch feed pipeline, and the meeting point with the second branch feed pipeline is downstream of the second valve, and a third valve is arranged on the pre-fractionation discharge pipeline; A heating furnace connected to the raw material tank; A reactor connected to the heating furnace, wherein a catalyst is contained in the reactor; A gas-liquid separator connected to the reactor; a stripping tower connected to the gas-liquid separator; as well as The fractionation tower is connected to the stripping tower, and the fractionation tower is connected to a refined naphtha discharge pipeline.
2. A naphtha hydrogenation system with switchable process flow according to claim 1, characterized in that: The second valve is configured as a flow regulating valve.
3. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: A raw material pump is provided between the raw material tank and the heating furnace.
4. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The stripping tower is connected with an acid gas discharge pipeline.
5. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The top of the pre-fractionation tower is connected to a light naphtha discharge pipeline.
6. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The top of the fractionation tower is connected with a second type of light naphtha discharge pipeline.
7. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The feed temperature of the pre-fractionation tower is 90-120°C, the top pressure is 0.08-0.15MpaG, and the bottom temperature is 135-140°C.
8. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The feed rate of the reactor is 400-600 t / h, the reaction temperature is 280-330°C, the space velocity is 5.5 / h, and the reaction pressure is 2.7-3.0 MpaG.
9. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The feed temperature of the stripping tower is 150-158°C, the top pressure is 0.8-0.83MpaG, and the bottom temperature is 185-190°C.
10. A naphtha hydrogenation system with switchable process flow according to claim 1 or 2, characterized in that: The feed temperature of the fractionation tower is 120-130°C, the top pressure is 0.08-0.15MpaG, and the bottom temperature is 140-150°C.