Pressure reduction structure for refining rich aromatic hydrocarbon

Abstract

The utility model discloses a pressure reduction structure for refining rich aromatic hydrocarbon, which relates to the technical field of needle coke, is arranged between a rich aromatic hydrocarbon refining device and a needle coke device, and comprises a heating furnace and a pressure reduction device, the vacuum tower is connected with the heating furnace, so that the refined rich aromatic hydrocarbon enters the heating furnace after being heated to a proper temperature; the vacuum unit is connected with the vacuum tower; the feeding end of the side line pump is connected with the side part of the vacuum tower so as to guide out the separated light components; the oil evaporator is connected with the discharge end of the side pump; and the cooling assembly is connected with the oil evaporator so as to reduce the temperature of the separated light components. According to the utility model, light components in refined rich aromatic hydrocarbon can be separated, so that part of light components are prevented from being cracked into dry gas, economic benefits are increased, the temperature of the fractionating tower bottom of the needle coke device is increased, and the enrichment degree of tricyclic and tetracyclic aromatic hydrocarbon beneficial to production of high-quality needle coke in the refined rich aromatic hydrocarbon components is increased; and the quality of the needle coke is further improved.

Description

TECHNICAL FIELD

[0001] The utility model relates to needle coke technical field, specifically, relate to a pressure reducing structure of refined aromatic hydrocarbon. BACKGROUND

[0002] Needle coke is the strategic raw material of modern industry, and is mainly applied to the production of high-end industrial carbon products, refined aromatic hydrocarbon obtained in the production process of needle coke is directly introduced into needle coke device for subsequent processing operation, which causes the following problems:

[0003] 1, 5-15% light components exist in refined aromatic hydrocarbon, and after entering the needle coke device fractionating column, part of heat is taken away from the bottom of the needle coke device fractionating column, which results in low temperature of the bottom of the needle coke device fractionating column, and increases the consumption of fuel;

[0004] 2, the light components exist in the needle coke device coke tower and further crack to produce a large amount of dry gas, which reduces the economic benefit;

[0005] 3, the existence of light components reduces the proportion of three-ring and four-ring aromatic hydrocarbons in refined aromatic hydrocarbon, which is beneficial to the production of high-quality needle coke. CONTENT OF UTILITY MODEL

[0006] The utility model discloses a pressure reducing structure of refined aromatic hydrocarbon to separate the light components existing in refined aromatic hydrocarbon.

[0007] The utility model solves the technical scheme that its technical problem adopts:

[0008] A pressure reducing structure of refined aromatic hydrocarbon is arranged between the refined aromatic hydrocarbon device and the needle coke device,

[0009] Including:

[0010] Heating furnace;

[0011] Vacuum tower is connected with the heating furnace, so that refined aromatic hydrocarbon is heated to the appropriate temperature and then enters the vacuum tower;

[0012] Vacuum unit is connected with the vacuum tower;

[0013] Side line pump, the feeding end is connected with the side of the vacuum tower, so that the separated light components are guided out;

[0014] Oil evaporator is connected with the discharge end of the side line pump;

[0015] Cooling assembly is connected with the oil evaporator to reduce the temperature of the separated light components.

[0016] Further, the heating furnace heats the refined aromatic hydrocarbon-rich material to 310-330 DEG C, providing necessary heat energy for subsequent separation.

[0017] Further, the cooling assembly comprises:

[0018] A water cooler connected to the oil evaporator;

[0019] An air cooler connected to the water cooler;

[0020] The water cooling and air cooling of the light component has the advantages of higher cooling efficiency, better resource utilization, greater system flexibility, longer equipment life, and environmental protection.

[0021] Further, the heating furnace is connected with a heat exchanger at the feeding end, and the refined aromatic hydrocarbon-rich material enters the heating furnace after the heat exchanger, so as to reduce the load during use of the heating furnace and save part of fuel.

[0022] Further, the bottom of the vacuum tower is connected with the heat exchange gas through a bottom line pump, so as to guide the heavy component at the bottom of the vacuum tower into the heat exchanger.

[0023] Further, the feeding end of the heat exchanger is connected with the discharging end of the refined aromatic hydrocarbon-rich material device, and the feeding end of the heat exchanger is connected with the feeding end of the needle coke device.

[0024] Further, the discharging end of the air cooler is connected with a storage tank, so as to realize preservation and storage of the light component separated by the vacuum separation.

[0025] Further, the storage tank is a light-shielded stainless steel or glass container, and the preservation temperature is less than 8 DEG C, so that the light component is more stable at a lower temperature, and the risk of volatile loss and chemical change is reduced.

[0026] Compared with the prior art, the utility model has the advantages of:

[0027] The utility model discloses be provided between the refining rich aromatic hydrocarbon device and the needle coke device, through the cooperation setting of heating furnace, pressure reduction tower, vacuum unit, side line pump, oil evaporator and cooling assembly, make the refining rich aromatic hydrocarbon can be effectively separated out light component under not carrying out cracking, thereby the valuable heavy aromatic hydrocarbon such as tricyclic and tetra cyclic aromatic hydrocarbon is protected, the light component is separated out after the refining rich aromatic hydrocarbon enters pressure reduction structure, avoids part light component to be cracked into dry gas, increases economic benefit, improves needle coke device fractionating tower bottom temperature at the same time, improves the enrichment degree of tricyclic, tetra cyclic aromatic hydrocarbon in the refining rich aromatic hydrocarbon component, which is favorable for producing high-quality needle coke, and further improves the quality of needle coke, and the light component separated out is cooled and exported pressure reduction tower under the action of side line pump, oil evaporator and cooling assembly, greatly improves the production effect of subsequent needle coke. BRIEF DESCRIPTION OF DRAWINGS

[0028] Figure 1 It is the structural schematic diagram of the utility model;

[0029] Figure 2 It is the installation position schematic diagram of heat exchanger;

[0030] Figure 3 It is the installation position schematic diagram of bottom line pump;

[0031] Figure 4 It is the installation position schematic diagram of storage tank;

[0032] Among them: 1, heating furnace;2, pressure reduction tower;3, vacuum unit;4, side line pump;5, oil evaporator;6, cooling assembly;61, water cooler;62, air cooler;7, heat exchanger;8, bottom line pump;9, storage tank. DETAILED DESCRIPTION

[0033] The technical scheme in the embodiments of the utility model will be described clearly and completely below in combination with the drawings in the embodiments of the utility model, and obviously, the described embodiments are only part of the embodiments of the utility model, not all the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by the person skilled in the art without creative labor belong to the protection scope of the utility model. The utility model is further illustrated in combination with the drawings and embodiments:

[0034] Embodiment 1:

[0035] Referring to the drawings, Figure 1 The utility model discloses a pressure reduction structure of refining rich aromatic hydrocarbon, including:

[0036] Heating furnace 1 is used for the entry of refining rich aromatic hydrocarbon, and the refining rich aromatic hydrocarbon is heated to 310-330 DEG C;

[0037] The reduced pressure tower 2 is connected with the heating furnace 1, so that the refined aromatic hydrocarbon is heated to a suitable temperature and then enters the reduced pressure tower 2;

[0038] The vacuum unit 3 is connected with the reduced pressure tower 2, so as to provide a low pressure environment for the reduced pressure tower 2, so that the distillation process can be carried out efficiently at a lower temperature, and the quality of the refined aromatic hydrocarbon is protected;

[0039] The side line pump 4 is connected with the side of the reduced pressure tower 2 at the feeding end, so as to guide the separated light components out of the reduced pressure tower 2 and prevent them from entering the subsequent processing process;

[0040] The oil evaporator 5 is connected with the discharging end of the side line pump 4, so that the light components can be further evaporated at a certain temperature, which is helpful to the purity and quality;

[0041] The cooling assembly 6 is connected with the oil evaporator 5, so that the separated light components can be cooled to reduce the temperature, reduce the volatility and explosion risk, ensure the safety of the subsequent processing and storage, and the cooled light components are easier to be liquefied or kept in a liquid state, which is beneficial to storage and transportation.

[0042] In the embodiment, by adding the reduced pressure structure between the refined aromatic hydrocarbon device and the needle coke device, the light components can be effectively separated without cracking, so that the valuable heavy aromatic hydrocarbons such as triphenyl and tetraphenyl are protected; the light components can be separated from the refined aromatic hydrocarbon after entering the reduced pressure structure, so that part of the light components are not cracked into dry gas, the economic benefit is increased, the temperature of the fractionating tower bottom of the needle coke device is increased, the enrichment degree of the triphenyl and tetraphenyl in the refined aromatic hydrocarbon component which is beneficial to the production of high-quality needle coke is increased, and the quality of the needle coke is improved; and the separated light components are cooled and discharged out of the reduced pressure tower 2 by the side line pump 4, the oil evaporator 5 and the cooling assembly 6.

[0043] For the structure of the cooling assembly 6 in the above embodiment, specifically:

[0044] Referring to FIG. 1, Figure 1 the cooling assembly 6 includes:

[0045] The water cooler 61 is connected with the oil evaporator 5;

[0046] The air cooler 62 is connected with the water cooler 61;

[0047] In the scheme, the cooling assembly 6 can make the light components rapidly reduce the temperature through the water cooler 61, and the air cooler 62 can provide stable cooling effect for a long time, which helps to maintain the long-term operation stability of the system, and the air cooler 62 provides additional cooling support. Among them, the advantages of using water cooling and air cooling together for the light components are that it can provide higher cooling efficiency, better resource utilization, greater system flexibility and longer equipment life, while also meeting the needs of environmental protection.

[0048] Embodiment 2:

[0049] The difference from embodiment 1 is that:

[0050] Referring to FIG. 2, the heat furnace 1 is connected with a heat exchanger 7 at the feeding end, and the refined aromatic-rich hydrocarbon enters the heat furnace 1 through the heat exchanger 7 to reduce the load during the use of the heat furnace 1, thereby saving part of the fuel. Figure 2 In the scheme, the heat exchanger 7 can use the waste heat from the outlet of the heat furnace 1 or other high-temperature process fluid to preheat the refined aromatic-rich hydrocarbon entering the heat furnace 1, which not only increases the feeding temperature and reduces the fuel consumption required by the heat furnace 1, but also improves the energy efficiency of the whole system. Through the preheating of the heat exchanger 7, the feeding temperature can be closer to the operating temperature of the heat furnace 1, thereby reducing the stress and damage to the equipment caused by sudden temperature changes.

[0051] Embodiment 3:

[0052] The difference from embodiment 2 is that:

[0053] Referring to FIG. 3, the bottom of the vacuum tower 2 is connected with the heat exchange gas through a bottom line pump 8 to guide the heavy components at the bottom of the vacuum tower 2 into the heat exchanger 7. At the same time, the feeding end of the heat exchanger 7 is connected with the discharge end of the refined aromatic-rich hydrocarbon device, so that the refined aromatic-rich hydrocarbon produced by the refined aromatic-rich hydrocarbon device directly enters the heat exchanger 7, and then the vacuum process begins. The feeding end of the heat exchanger 7 is connected with the feeding end of the needle coke device, so that the heavy components separated by the vacuum tower 2 are directly introduced into the needle coke device for the next operation after being heated by the heat exchanger 7.

[0054] Figure 3 Embodiment 4:

[0055] The difference from embodiment 3 is that:

[0056] Referring to FIG. 4, the bottom of the vacuum tower 2 is connected with the heat exchange gas through a bottom line pump 8 to guide the heavy components at the bottom of the vacuum tower 2 into the heat exchanger 7. At the same time, the feeding end of the heat exchanger 7 is connected with the discharge end of the refined aromatic-rich hydrocarbon device, so that the refined aromatic-rich hydrocarbon produced by the refined aromatic-rich hydrocarbon device directly enters the heat exchanger 7, and then the vacuum process begins. The feeding end of the heat exchanger 7 is connected with the feeding end of the needle coke device, so that the heavy components separated by the vacuum tower 2 are directly introduced into the needle coke device for the next operation after being heated by the heat exchanger 7.

[0057] Referring to FIG. 4, the bottom of the vacuum tower 2 is connected with the heat exchange gas through a bottom line pump 8 to guide the heavy components at the bottom of the vacuum tower 2 into the heat exchanger 7. At the same time, the feeding end of the heat exchanger 7 is connected with the discharge end of the refined aromatic-rich hydrocarbon device, so that the refined aromatic-rich hydrocarbon produced by the refined aromatic-rich hydrocarbon device directly enters the heat exchanger 7, and then the vacuum process begins. The feeding end of the heat exchanger 7 is connected with the feeding end of the needle coke device, so that the heavy components separated by the vacuum tower 2 are directly introduced into the needle coke device for the next operation after being heated by the heat exchanger 7. Figure 4 ​As shown, the air cooler 62 is connected with a storage tank 9 at the discharge end to realize the preservation storage operation of the light components separated by the pressure reduction.

[0058] The basic principle, main features and advantages of the present application are shown and described above. Those skilled in the art should understand that the present application is not limited by the above examples, and the above embodiments and descriptions in the specification are only to illustrate the principle of the present application. Without departing from the spirit and scope of the present application, various changes and improvements can be made to the present application, and these changes and improvements all fall within the scope of the present application. The scope of protection of the present application is defined by the appended claims and their equivalents.

Claims

1. A vacuum structure for refining aromatic hydrocarbons, disposed between an aromatic hydrocarbon refining unit and a needle coke unit, characterized in that: include: Heating furnace (1); The pressure reducing tower (2) is connected to the heating furnace (1) so that the refined aromatic hydrocarbons are heated to a suitable temperature before entering the furnace; The vacuum unit (3) is connected to the pressure reducing tower (2); A side-stream pump (4) is connected at its feed end to the side of the pressure reducing tower (2) to discharge the separated light components; The oil evaporator (5) is connected to the discharge end of the side-line pump (4); The cooling assembly (6) is connected to the oil evaporator (5) to reduce the temperature of the separated light components.

2. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 1, characterized in that: The heating furnace (1) heats the refined aromatic hydrocarbons to 310-330°C.

3. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 1, characterized in that: The cooling assembly (6) includes: A water cooler (61) is connected to an oil evaporator (5); An air cooler (62) is connected to a water cooler (61).

4. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 3, characterized in that: The heating furnace (1) is connected to a heat exchanger (7) at the feed end, and the refined aromatic hydrocarbons enter the heating furnace (1) after passing through the heat exchanger (7).

5. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 4, characterized in that: The bottom of the pressure reducing tower (2) is connected to the heat exchange gas via a bottom pump (8) so that the heavy components at the bottom of the pressure reducing tower (2) are introduced into the heat exchanger (7).

6. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 5, characterized in that: The feed end of the heat exchanger (7) is connected to the discharge end of the refined aromatic hydrocarbon unit, and the feed end of the heat exchanger (7) is connected to the feed end of the needle coke unit.

7. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 6, characterized in that: The air cooler (62) is connected to a storage tank (9) at its discharge end.

8. The vacuum-reduced structure for refining aromatic hydrocarbons according to claim 7, characterized in that: The storage tank (9) is a light-proof stainless steel or glass container, and the storage temperature is less than 8°C.

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