Production system of pentane foaming agent

Abstract

The utility model provides a production system of a pentane foaming agent. The production system comprises an n-isomerization separation device, a naphtha hydrogenation device, a diesel oil hydrocracking device and a storage and transportation device, wherein the input end of the normal and isomerous separation device is connected with the output end of the diesel hydrocracking device, and the output end of the normal and isomerous separation device is connected with the input end of the storage and transportation device; the output end of the naphtha hydrogenation device is connected with the input end of the storage and transportation device; the output end of the diesel hydrocracking device is respectively connected with the input end of the normal and isomerous separation device and the input end of the storage and transportation device. According to the utility model, the topped oil prepared by naphtha hydrogenation and the light naphtha produced by the diesel oil hydrocracking device are introduced into the n-isomerization separation device, and isopentane and n-pentane in the topped oil and the light naphtha are processed and utilized, so that a pentane foaming agent product with high additional value is produced; the utility model aims to improve the added value of a light naphtha product and improve the inventory of isopentane.

Description

Technical Field

[0001] The utility model relates to the technical field of petrochemical industry, and particularly relates to a production system of pentane foaming agent. Background Art

[0002] At present, in petrochemical production, the content of isopentane in the raw material light naphtha is 19.26% higher than the design value. In order to maximize the product added value, increase economic benefits, and solve the problems such as high inventory of isopentane, the production of pentane foaming agent products can be selected; there are six models of pentane foaming agent from F3 to F8. The ratio of isopentane to n-pentane in the light naphtha of the diesel hydrocracking unit is 58.0:9.8, and the ratio of isopentane to n-pentane in the naphtha hydrotreating debutanizer is 27.4:40.2. The feed ratio of debutanizer to diesel light naphtha is 1.3:1, which is suitable for producing F4 type foaming agent (n-pentane:isopentane = 4:6).

[0003] It should be noted that the information disclosed in the above background art section is only used to strengthen the understanding of the background of the present utility model and does not constitute any limitation to the present utility model. Summary of the Utility Model

[0004] In view of the above-mentioned disadvantages of the prior art, the present utility model provides a production system of pentane foaming agent. By introducing the debutanizer prepared by naphtha hydrotreating and the light naphtha produced by the diesel hydrocracking unit into the normal and isomer separation device, the isopentane and n-pentane in the debutanizer and light naphtha are processed and utilized to produce high-value-added pentane foaming agent products, so as to solve the problems of improving the added value of light naphtha products and high inventory of isopentane.

[0005] The present utility model provides a production system of pentane foaming agent, including a normal and isomer separation device, a naphtha hydrotreating device, a diesel hydrocracking device and a storage and transportation device; wherein, the input end of the normal and isomer separation device is connected with the output end of the diesel hydrocracking device, and the output end of the normal and isomer separation device is connected with the input end of the storage and transportation device; the output end of the naphtha hydrotreating device is connected with the input end of the storage and transportation device; the output end of the diesel hydrocracking device is respectively connected with the input end of the normal and isomer separation device and the input end of the storage and transportation device.

[0006] In an embodiment of the present utility model, the normal and isomer separation device includes a buffer tank, an isopentane stripper, an n-pentane stripper and an isohexane stripper; the input ports and output ports of the buffer tank, the isopentane stripper, the n-pentane stripper and the isohexane stripper are connected in sequence along the flow direction of the material in the normal and isomer separation device.

[0007] In an embodiment of the present utility model, the input port of the buffer tank is connected with the output end of the diesel hydrocracking device and the output end of the storage and transportation device; the output port of the isohexane stripper is connected with the input end of the storage and transportation device.

[0008] In an embodiment of the present utility model, the isopentane column includes two output ports, one output port is connected to the normal pentane column, and the other output port is connected to the input end of the storage and transportation device.

[0009] In an embodiment of the present utility model, the normal pentane column includes two output ports, one output port is connected to the isohexane column, and the other output port is connected to the output end of the isopentane column and also connected to the input end of the storage and transportation device.

[0010] In an embodiment of the present utility model, the storage and transportation device includes an isopentane tank, an HC light naphtha tank, and an ethylene feedstock naphtha tank; the isopentane tank, the HC light naphtha tank, and the ethylene feedstock naphtha tank are independent of each other and are respectively connected to at least one of the output ends of the normal and isomeric separation device, the naphtha hydrogenation device, and the diesel hydrocracking device.

[0011] In an embodiment of the present utility model, the input end of the isopentane tank is respectively connected to the output ends of the isopentane column and the normal pentane column through a pentane foaming agent output pipeline.

[0012] In an embodiment of the present utility model, it further includes a first raw material input line, the first raw material input line is connected to the output end of the naphtha hydrogenation device, and the first raw material input line includes a first raw material first input branch line connected to the ethylene feedstock naphtha tank and a first raw material second input branch line connected to the HC light naphtha tank.

[0013] In an embodiment of the present utility model, it further includes a second raw material input line, the second raw material input line is connected to the output end of the diesel hydrocracking device, and the second raw material input line includes a second raw material first input branch line connected to the buffer tank and a second raw material second input branch line connected to the first raw material input line.

[0014] In an embodiment of the present utility model, it further includes a C6+ naphtha output pipeline, and the C6+ naphtha output pipeline is connected between the output end of the isohexane column and the input end of the ethylene feedstock naphtha tank.

[0015] Advantages of the present utility model: By combining the diesel hydrocracking device, the naphtha hydrogenation device, and the normal and isomeric separation device, the topped oil prepared by naphtha hydrogenation and the light naphtha produced by the diesel hydrocracking device are introduced into the normal and isomeric separation device, and the isopentane and normal pentane in the topped oil and light naphtha are processed and utilized to produce high-value-added pentane foaming agent products, increasing economic benefits.

[0016] It should be understood that the above general description and the following detailed description are only exemplary and explanatory, and cannot limit the present utility model. Brief Description of the Drawings

[0017] The accompanying drawings here are incorporated into the specification and form a part of this specification, showing embodiments in line with the present utility model, and are used together with the specification to explain the principles of the present utility model. Obviously, the accompanying drawings in the following description are only some embodiments of the present utility model. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts. In the drawings:

[0018] Figure 1 is a pipeline diagram of the pentane foaming agent production system in the present utility model;

[0019] Figure 2 is a pipeline diagram of the normal and isomer separation device in the present utility model.

[0020] In the figure: 11, naphtha hydrogenation unit; 12, first raw material input line; 121, first first input branch line of the first raw material; 122, first second input branch line of the first raw material; 13, second raw material input line; 131, first first input branch line of the second raw material; 132, second second input branch line of the second raw material; 14, buffer tank; 15, isopentane tower; 16, n-pentane tower; 17, isohexane tower; 18, C6+ naphtha output pipeline; 19, normal and isomer separation device; 20, pentane foaming agent output pipeline; 21, isopentane tank; 22, HC light naphtha tank; 23, ethylene feed naphtha tank; 24, storage and transportation device; 25, diesel hydrocracking unit. Detailed implementation manners

[0021] The following uses specific examples to illustrate the implementation manners of the present utility model. Those skilled in the art can easily understand other advantages and effects of the present utility model from the content disclosed in this specification. The present utility model can also be implemented or applied through other different specific implementation manners. Various details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of the present utility model. It should be noted that, without conflict, the following embodiments and the features in the embodiments can be combined with each other. It should also be understood that the terms used in the embodiments of the present utility model are for the purpose of describing specific implementation manners and not for limiting the protection scope of the present utility model.

[0022] Please refer to Figures 1 to 2It should be noted that the structures, proportions, sizes, etc. shown in the drawings of this specification are only used to cooperate with the content disclosed in the specification for those familiar with this technology to understand and read, and are not used to limit the conditions for the implementation of the present utility model. Therefore, they do not have substantial technical significance. Any modification of the structure, change in the proportional relationship, or adjustment of the size, without affecting the effects that the present utility model can produce and the purposes that can be achieved, should still fall within the scope covered by the technical content disclosed in the present utility model. At the same time, the terms such as the positions and quantitative relationships cited in this specification are only for the convenience of clear narration and are not used to limit the scope for the implementation of the present utility model. The change or adjustment of their relative relationships, without substantial change in the technical content, should also be regarded as the scope within which the present utility model can be implemented.

[0023] In the production process of pentane foaming agent, the content of isopentane in the raw material light naphtha is 19.26% higher than the designed value. In the downstream application of isopentane, isopentane is used for gasoline blending, and most of the remaining isopentane is sold as low-value-added products. The present utility model provides a production system for pentane foaming agent. By combining a diesel hydrocracking unit, a naphtha hydrotreating unit, and a normal and isomer separation unit, the topped oil prepared by naphtha hydrotreating and the light naphtha produced by the diesel hydrocracking unit are led to the normal and isomer separation unit to process and utilize the isopentane and n-pentane in the topped oil and light naphtha, produce high-value-added pentane foaming agent products, and increase economic benefits.

[0024] Please refer to Figure 1 , the present utility model provides a production system for pentane foaming agent, including a normal and isomer separation unit 19, a naphtha hydrotreating unit 11, a diesel hydrocracking unit 25, and a storage and transportation unit 24; wherein, the input end of the normal and isomer separation unit 19 is connected to the output end of the diesel hydrocracking unit 25, the output end of the normal and isomer separation unit 19 is connected to the input end of the storage and transportation unit 24; the output end of the naphtha hydrotreating unit 11 is connected to the input end of the storage and transportation unit 24; the output end of the diesel hydrocracking unit 25 is respectively connected to the input end of the normal and isomer separation unit 19 and the input end of the storage and transportation unit 24.

[0025] In the embodiment of the present utility model, in the production process of pentane foaming agent, the content of isopentane in the raw material light naphtha is 19.26% higher than the designed value. In the downstream application of isopentane, isopentane is used for gasoline blending, and most of the remaining isopentane is sold as low-value-added products. By combining the diesel hydrocracking unit 25, the naphtha hydrotreating unit 11, and the normal and isomer separation unit 19, the topped oil prepared by naphtha hydrotreating and the light naphtha produced by the diesel hydrocracking unit 25 are led to the normal and isomer separation unit 19 to process and utilize the isopentane and n-pentane in the topped oil and light naphtha, produce high-value-added pentane foaming agent products, and increase economic benefits.

[0026] Specifically, in the topped oil produced by the naphtha hydrogenation unit 11, the contents of isopentane, n-pentane, isohexane, and n-hexane respectively account for, for example, 27.4, 40.2, 15.4, and 9.54 wt%, and the isopentane and n-pentane in the topped oil are good raw materials for separation by the normal and isomer separation unit 19, having good separation efficiency and can be processed and utilized.

[0027] More specifically, in the light naphtha produced by the diesel hydrocracking unit 25, the contents of isopentane, n-pentane, isohexane, and n-hexane respectively account for, for example, 58.0, 9.8, 28.05, and 0.99 wt%, and the isopentane and n-pentane in the light naphtha are good raw materials for separation by the normal and isomer separation unit 19, having good separation efficiency and can be processed and utilized.

[0028] Further, the normal and isomer separation unit 19 includes a buffer tank 14, an isopentane stripper 15, an n-pentane stripper 16, and an isohexane stripper 17; the input and output ports of the buffer tank 14, the isopentane stripper 15, the n-pentane stripper 16, and the isohexane stripper 17 are connected in sequence along the flow direction of the material in the normal and isomer separation unit 19.

[0029] The input port of the buffer tank 14 is connected to the output end of the diesel hydrocracking unit 25 and the output end of the storage and transportation unit 24; the output port of the isohexane stripper 17 is connected to the input end of the storage and transportation unit 24.

[0030] The isopentane stripper 15 includes two output ports, one output port is connected to the n-pentane stripper 16, and the other output port is connected to the input end of the storage and transportation unit 24.

[0031] The n-pentane stripper 16 includes two output ports, one output port is connected to the isohexane stripper 17, and the other output port is connected to the output end of the isopentane stripper 15 and is connected to the input end of the storage and transportation unit 24.

[0032] Further, in this embodiment, the input end of the isopentane stripper 15 is connected to the output end of the buffer tank 14, and the output end of the isopentane stripper 15 is connected to the input end of the n-pentane stripper 16. In the isopentane stripper 15, the isopentane in the raw material is separated out.

[0033] The input end of the n-pentane stripper 16 is connected to the output end of the isopentane stripper 15, and the output end of the n-pentane stripper 16 is connected to the input end of the isohexane stripper 17. In the n-pentane stripper 16, the n-pentane in the raw material is separated out.

[0034] The input end of the isohexane stripper 17 is connected to the output end of the n-pentane stripper 16, and the output end of the isohexane stripper 17 is connected to the input end of the ethylene feedstock naphtha tank 23. In the isohexane stripper 17, the C6+ naphtha product is used as the raw material for ethylene and is fed to the ethylene cracking unit through the ethylene feedstock naphtha tank 23.

[0035] The output end of the isopentane column 15 is connected to the output end of the n-pentane column 16, and the isopentane product output from the isopentane column 15 and the n-pentane product output from the n-pentane column 16 are mixed in a ratio of 6:4 to produce a pentane foaming agent product.

[0036] Furthermore, the storage and transportation device 24 includes an isopentane tank 21, an HC light naphtha tank 22, and an ethylene feedstock naphtha tank 23; the isopentane tank 21, the HC light naphtha tank 22, and the ethylene feedstock naphtha tank 23 are independent of each other and are respectively connected to at least one of the output end of the normal and isomer separation device 19, the output end of the naphtha hydrogenation device 11, and the output end of the diesel hydrocracking device 25.

[0037] The input end of the isopentane tank 21 is respectively connected to the output ends of the isopentane column 15 and the n-pentane column 16 through the pentane foaming agent output pipeline 20.

[0038] The production system further includes a first raw material input line 12, and the first raw material input line 12 is connected to the output end of the naphtha hydrogenation device 11. The first raw material input line 12 includes a first raw material first input branch line 121 connected to the ethylene feedstock naphtha tank 23 and a first raw material second input branch line 122 connected to the HC light naphtha tank 22. That is, the first raw material input pipeline is connected to the input end of the storage and transportation device 24 to transport raw materials to the normal and isomer separation device 19. Among them, the first raw material input pipeline transports, for example, topped oil as raw materials.

[0039] The production system further includes a second raw material input line 13, and the second raw material input line 13 is connected to the output end of the diesel hydrocracking device 25. The second raw material input line 13 includes a second raw material first input branch line 131 connected to the buffer tank 14 and a second raw material second input branch line 132 connected to the first raw material input line 12. The second raw material input pipeline is connected to the input end of the normal and isomer separation device 19 to transport raw materials to the normal and isomer separation device 19. Among them, the second raw material input pipeline transports, for example, light naphtha as raw materials.

[0040] The production system further includes a C6+ naphtha output pipeline, and the C6+ naphtha output pipeline is connected between the output end of the deisohexane column 17 and the input end of the ethylene feedstock naphtha tank 23.

[0041] Specifically, the normal and isomer separation unit 19 is connected to the diesel hydrocracking unit 25 and the storage and transportation unit 24. In this embodiment, the light naphtha from the diesel hydrocracking unit 25 and the topped oil from the storage and transportation unit 24 are mixed as the raw material of the normal and isomer separation unit 19. In the deisopentane tower 15 of the normal and isomer separation unit 19, the isopentane fraction is separated from the top of the rectification tower, and the bottom fraction enters the depentane tower 16 to separate the n-pentane fraction. After the isopentane (n-pentane mass fraction 58% - 62%) and n-pentane (n-pentane mass fraction 38% - 42%) are mixed, a pentane foaming agent product with high added value is produced and sent to the isopentane tank 21, where a small amount is used for gasoline blending and most is sold externally to improve economic benefits.

[0042] Please refer to Figure 2 , in an embodiment, in the production system of the pentane foaming agent, the production process of its normal and isomer separation unit includes the following steps:

[0043] Using hydrotreated topped naphtha and diesel hydrocracked light naphtha as raw materials, the raw materials are heated and pressurized from the raw material tank 1 and enter the deisopentane tower 2 through the 66th, 70th or 74th tray. After the raw materials are rectified in the deisopentane tower, a part of the overhead material enters the reflux drum I and returns to the deisopentane tower 1 through the first tray of the deisopentane tower 1, and the other part is collected to obtain isopentane. The bottom material of the tower enters the depentane tower 2 for rectification;

[0044] The bottom material of the deisopentane tower 1 enters the depentane tower 2 through the 62nd, 66th or 70th tray. After being rectified in the depentane tower 2, a part of the overhead material enters the reflux drum II and returns to the depentane tower 2 through the first tray of the depentane tower 2, and the other part is collected to obtain n-pentane, which is mixed with the isopentane from the top of the deisopentane tower at a ratio of 4:6 to produce a pentane foaming agent. The bottom material of the tower enters the deisohexane tower 6 (the deisohexane tower 6 is used as a buffer tank) and is pumped to the ethylene cracking as a raw material through the bottom pump of the deisohexane tower.

[0045] In this embodiment, the normal and isomer separation unit saves the operation of the deisohexane tower on the basis of the original three-tower process by optimizing the cross-line of the products at the top of the deisopentane tower and the top of the depentane tower (the pipeline represented by the red line in the attachment) Figure 2 , and realizes the conversion of naphtha into a pentane foaming agent product with high added value through two towers; it is both energy-saving, solves the problem of high isopentane inventory, and reduces the safety risk.

[0046] More specifically, compared with the original scheme of processing light naphtha, the consumption of utilities in this embodiment is shown in Table 1: The consumption of utilities in this embodiment is shown in Table 2:

[0047] Table 1

[0048]

[0049] Table 2

[0050]

[0051] As can be seen from the above table, in the production system of the normal and isomeric separation device adopting the solution of this embodiment, although the steam consumption of the isopentane tower and the normal pentane tower has increased slightly, the steam consumption of the normal pentane tower is avoided, and thus the overall steam consumption and its power consumption of the normal and isomeric separation device are significantly reduced, achieving energy conservation and emission reduction.

[0052] In summary, the present utility model provides a production system for pentane foaming agent. By combining a diesel hydrocracking unit, a naphtha hydrotreating unit, and a normal and isomeric separation device, the topped oil prepared by naphtha hydrotreating and the light naphtha produced by the diesel hydrocracking unit are introduced into the normal and isomeric separation device, and the isopentane and normal pentane in the topped oil and light naphtha are processed and utilized to produce pentane foaming agent products with high added value, increasing economic benefits.

[0053] The above embodiments are only illustrative of the principles and effects of the present utility model, and are not intended to limit the present utility model. Any person familiar with this technology can modify or change the above embodiments without departing from the spirit and scope of the present utility model. Therefore, all equivalent modifications or changes made by those with ordinary knowledge in the technical field without departing from the spirit and technical idea disclosed by the present utility model should still be covered by the claims of the present utility model.

Claims

1. A production system for a pentane blowing agent, characterized in that: It comprises a normal isomer separation device (19), a naphtha hydrogenation device (11), a diesel hydrocracking device (25) and a storage and transportation device (24); wherein the input end of the normal isomer separation device (19) is connected to the output end of the diesel hydrocracking device (25), and the output end of the normal isomer separation device (19) is connected to the input end of the storage and transportation device (24); the output end of the naphtha hydrogenation device (11) is connected to the input end of the storage and transportation device (24); and the output end of the diesel hydrocracking device (25) is respectively connected to the input end of the normal isomer separation device (19) and the input end of the storage and transportation device (24).

2. The production system according to claim 1, characterized in that: The normal isomerization separation device (19) comprises a buffer tank (14), a deisopentanizer (15), a de-normal pentanizer (16) and a deisohexanizer (17); the input port and the output port of the buffer tank (14), the deisopentanizer (15), the de-normal pentanizer (16) and the deisohexanizer (17) are connected in sequence along the flow direction of the material in the normal isomerization separation device (19).

3. The production system according to claim 2, characterized in that: The input port of the buffer tank (14) is connected to the output end of the diesel hydrocracking device (25) and the output end of the storage and transportation device (24); the output port of the deisohexanizer (17) is connected to the input end of the storage and transportation device (24).

4. The production system according to claim 2, characterized in that: The de-isopentanizer (15) comprises two output ports, one of which is connected to the de-normal pentanizer (16), and the other of which is connected to the input end of the storage and transportation device (24).

5. The production system according to claim 2, characterized in that: The de-normal pentane tower (16) comprises two output ports, one of which is connected to the de-isohexane tower (17), and the other of which is connected to the output end of the de-isopentane tower (15) and to the input end of the storage and transportation device (24).

6. The production system according to claim 2, characterized in that: The storage and transportation device (24) comprises an isopentane tank (21), an HC light naphtha tank (22) and an ethylene material naphtha tank (23); the isopentane tank (21), the HC light naphtha tank (22) and the ethylene material naphtha tank (23) are independent of each other and are respectively connected to at least one of the output ends of the normal isomerization separation device (19), the output end of the naphtha hydrogenation device (11) and the output end of the diesel hydrocracking device (25).

7. The production system according to claim 6, characterized in that: The input end of the isopentane tank (21) is connected to the output ends of the de-isopentane tower (15) and the de-normal pentane tower (16) respectively through a pentane foaming agent output pipeline (20).

8. The production system according to claim 6, characterized in that: It also includes a first raw material input line (12), which is connected to the output end of the naphtha hydrogenation unit (11), and the first raw material input line (12) includes a first raw material first input branch line (121) connected to the ethylene material naphtha tank (23) and a first raw material second input branch line (122) connected to the HC light naphtha tank (22).

9. The production system according to claim 8, characterized in that: It also includes a second raw material input line (13), which is connected to the output end of the diesel hydrocracking unit (25), and the second raw material input line (13) includes a second raw material first input branch line (131) connected to the buffer tank (14) and a second raw material second input branch line (132) connected to the first raw material input line (12).

10. The production system according to claim 6, characterized in that: It also includes a C6+ naphtha output pipeline, which is connected between the output end of the deisohexanizer (17) and the input end of the ethylene material naphtha tank (23).

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