Energy-saving styrene production device

Abstract

The utility model discloses an energy-saving styrene production device which comprises a device body, the device body comprises an alkylation unit, a rectification unit, an ethylbenzene dehydrogenation unit and a tank area unit, the rectification unit is arranged on the front side of the alkylation unit, the ethylbenzene dehydrogenation unit is arranged on one side of the alkylation unit, and the tank area unit is arranged on the other side of the alkylation unit. A storage tank I and a storage tank II are respectively arranged in the tank field unit, the alkylation unit comprises two alkylation reactors, a pre-fractionating tower and a non-aromatic removal tower, and a gas inlet pipe is arranged on the outer wall of the alkylation reactor on the left side; a diethylbenzene pipe is arranged below the gas inlet pipe, one end of the diethylbenzene pipe is arranged at the bottom of the alkylation reactor on the right side, a first connecting pipe is arranged at the upper end of the alkylation reactor, one end of the first connecting pipe is connected to a pre-fractionating tower, and a non-aromatic removal tower is arranged on one side of the pre-fractionating tower; the stability of styrene production and the high efficiency of styrene dehydrogenation can be improved, and the method has practicability.

Description

Technical Field

[0001] The utility model relates to the technical field of styrene production, in particular to an energy-saving styrene production device. Background Art

[0002] Styrene distillation utilizes a process that requires only two heating cycles. Ethylbenzene and styrene are first separated in a crude styrene column. The benzene, toluene, and ethylbenzene at the top of the column then enter the ethylbenzene column to separate benzene and toluene from ethylbenzene. Benzene and toluene then enter the benzene-toluene column for further separation. The bottoms of the crude styrene column enter the refined styrene column. Because the ratio of ethylbenzene and water azeotropes is constant, the steam flow at the steam superheater outlet cannot be varied while maintaining a constant total water-hydrocarbon ratio. To achieve a specific reaction temperature, the steam superheater outlet temperature must be increased. Currently, the steam superheater outlet temperature for this process is above 900°C, presenting significant challenges to process operation and engineering design.

[0003] There are certain problems in the production of existing styrene. It is often not stable enough during the production process, and it is difficult to produce styrene with high purity. In addition, the production process is relatively complicated, the operation is troublesome, and the energy-saving effect is relatively poor. In response to the above problems, a styrene energy-saving production device is proposed for improvement and upgrading. Utility Model Content

[0004] The purpose of the utility model is to provide an energy-saving styrene production device to solve the problems raised in the above background technology.

[0005] To solve the above problems, the following technical solutions are provided:

[0006] A styrene energy-saving production device is designed, including a device body, which includes a alkylation unit, a distillation unit, an ethylbenzene dehydrogenation unit and a tank area unit. The distillation unit is arranged in front of the alkylation unit, and the ethylbenzene dehydrogenation unit is arranged on one side of the alkylation unit. Storage tank 1 and storage tank 2 are respectively arranged inside the tank area unit.

[0007] Furthermore, the alkylation unit includes an alkylation reactor, a pre-fractionation tower and a de-aromatic tower. There are two alkylation reactors, and an air inlet pipe is provided on the outer wall of the left alkylation reactor. A diethylbenzene pipe is provided below the air inlet pipe, and one end of the diethylbenzene pipe is provided at the bottom of the right alkylation reactor.

[0008] Furthermore, a first connecting pipe is provided at the upper end of the alkylation reactor and one end of the first connecting pipe is connected to the pre-fractionation tower, a de-non-aromatic tower is provided on one side of the pre-fractionation tower, the bottom of the pre-fractionation tower is connected to the inside of the transport tank and a second connecting pipe is provided on the outer wall of the transport tank.

[0009] Furthermore, one end of the second connecting pipe is connected to the inside of the benzene tower body, a refined ethylbenzene tower is provided on one side of the benzene tower body and a diethylbenzene tower is provided on one side of the refined ethylbenzene tower, an air outlet pipe is provided on the outer wall of the diethylbenzene tower and one end of the air outlet pipe is connected to the storage tank.

[0010] Furthermore, the ethylbenzene dehydrogenation unit includes an ethylbenzene gas pipe, and one end of the ethylbenzene gas pipe is connected to the inside of the ethylbenzene steam separation tank. A dehydrogenation reactor 1 is provided in front of the ethylbenzene steam separation tank, and a dehydrogenation reactor 2 is provided in front of the dehydrogenation reactor 1.

[0011] Furthermore, a connecting pipe is provided on the second outer wall of the dehydrogenation reactor, and one end of the connecting pipe is connected to the ethylene separation tower, and a refined styrene tower is provided on one side of the ethylene separation tower.

[0012] Compared with the prior art, the beneficial effects of the present invention are:

[0013] 1. The utility model is provided with an alkylation unit, a distillation unit, an ethylbenzene dehydrogenation unit and a tank area unit in the device. Styrene is alkylated and dehydrogenated, and then the stabilized styrene gas is stored in a storage tank, thereby improving the stability of styrene production, simplifying the operation, and improving the efficiency of styrene dehydrogenation.

[0014] With reference to the following description and accompanying drawings, specific embodiments of the present invention are disclosed in detail, indicating how the principles of the present invention can be employed. It should be understood that the embodiments of the present invention are not limited in scope thereby. The embodiments of the present invention include numerous variations, modifications, and equivalents within the spirit and scope of the appended claims. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the embodiments of the present invention, they are used to explain the present invention and do not constitute a limitation of the present invention. In the accompanying drawings:

[0016] Figure 1 This is a schematic diagram of the overall structure of a styrene energy-saving production device of the utility model;

[0017] Figure 2 This is a side structural diagram of a styrene energy-saving production device of the present utility model;

[0018] Figure 3 for Figure 2 A schematic diagram of a partially enlarged split structure;

[0019] Figure 4 for Figure 2 A partial enlarged schematic diagram of the decomposed structure.

[0020] In the figure: 1. Device body; 2. Alkylation unit; 21. Air inlet pipe; 22. Alkylation reactor; 23. Pre-fractionation tower; 24. Diethylbenzene pipe; 25. First connecting pipe; 26. De-non-aromatic tower; 27. Transfer tank; 28. Second connecting pipe; 3. Distillation unit; 31. Benzene tower body; 32. Refined ethylbenzene tower; 33. Diethylbenzene tower; 34. Air outlet pipe; 4. Ethylbenzene dehydrogenation unit; 41. Ethylbenzene air pipe; 42. Ethylbenzene steam separation tank; 43. Dehydrogenation reactor 1; 44. Dehydrogenation reactor 2; 45. Ethylene separation tower; 46. Refined styrene tower; 5. Tank area unit; 51. Storage tank 1; 52. Storage tank 2. DETAILED DESCRIPTION

[0021] In order to make the technical means, creative features, objectives and effects achieved by the present invention easier to understand, the present invention is further described below in conjunction with specific implementation methods.

[0022] like Figure 1 - Figure 4 As shown, the present embodiment provides a design of an energy-saving styrene production device, including a device body 1, which includes a alkylation unit 2, a distillation unit 3, an ethylbenzene dehydrogenation unit 4 and a tank area unit 5. The distillation unit 3 is provided on the front side of the alkylation unit 2, and the ethylbenzene dehydrogenation unit 4 is provided on one side of the alkylation unit 2. The tank area unit 5 is respectively provided with a storage tank 1 51 and a storage tank 2 52.

[0023] Preferably, the alkylation unit 2 includes an alkylation reactor 22, a pre-fractionation tower 23 and a de-non-aromatic tower 26. There are two alkylation reactors 22, and an air inlet pipe 21 is provided on the outer wall of the left alkylation reactor 22. A diethylbenzene pipe 24 is provided below the air inlet pipe 21, and one end of the diethylbenzene pipe 24 is provided at the bottom of the right alkylation reactor 22. A first connecting pipe 25 is provided at the upper end of the alkylation reactor 22, and one end of the first connecting pipe 25 is connected to the pre-fractionation tower 23. A de-non-aromatic tower 26 is provided on one side of the pre-fractionation tower 23. The bottom of the pre-fractionation tower 23 is connected to the interior of a transport tank 27, and a second connecting pipe 28 is provided on the outer wall of the transport tank 27. One end of the second connecting pipe 28 is connected to the interior of a benzene tower body 31. A refined ethylbenzene tower 32 is provided on one side of the benzene tower body 31, and a diethylbenzene tower 33 is provided on one side of the refined ethylbenzene tower 32. An air outlet pipe 34 is provided on the outer wall of the diethylbenzene tower 33, and one end of the air outlet pipe 34 is connected to a storage tank 51.

[0024] Ethylene and benzene are processed by introducing them into two alkylation reactors 22 and a pre-fractionation tower 23. The hydrocarbonated liquid at the bottom of the pre-fractionation tower 23 is used as feed for the ethylbenzene distillation unit 3, and the hydrocarbonated liquid at the top is sent to the storage tank 51 in the intermediate tank area through the de-aromatic tower 26. The hydrocarbonated liquid enters the transfer tank 27 and is transported into the benzene tower body 31 through the second connecting pipe 28. Then, it flows along the conduit to the refined ethylbenzene tower 32 and then to the diethylbenzene tower 33. Benzene, refined ethylbenzene, diethylbenzene and polyethylbenzenes are produced in each tower in turn.

[0025] Preferably, the ethylbenzene dehydrogenation unit 4 includes an ethylbenzene gas pipe 41, and one end of the ethylbenzene gas pipe 41 is connected to the inside of an ethylbenzene steam separation tank 42, a dehydrogenation reactor 1 43 is provided on the front side of the ethylbenzene steam separation tank 42, a dehydrogenation reactor 2 44 is provided on the front side of the dehydrogenation reactor 1 43, a connecting pipe is provided on the outer wall of the dehydrogenation reactor 2 44, and one end of the connecting pipe is connected to an ethylene separation tower 45, and a refined styrene tower 46 is provided on one side of the ethylene separation tower 45.

[0026] Ethylbenzene feedstock flows through ethylbenzene dehydrogenation unit 4 along ethylbenzene gas pipe 41 into the ethylbenzene dehydrogenation separation tank to form an ethylbenzene azeotrope, thereby reducing the amount of water during the ethylbenzene dehydrogenation process. The azeotrope then enters dehydrogenation reactor 1 43 and dehydrogenation reactor 2 44 for dehydrogenation. The furnace oil after the reaction enters the distillation unit, and then enters ethylene separation tower 45 and refined styrene tower 46 in sequence. The ethylene in the towers is then sent to storage tank 2 52 in the tank area for storage, facilitating storage during styrene processing.

[0027] The principle and process of use of the present invention are as follows: first, ethylene and benzene are introduced into two alkylation reactors 22 and a pre-fractionation tower 23 for treatment. The hydrocarbonized liquid at the bottom of the pre-fractionation tower 23 is used as the feed for the ethylbenzene distillation unit 3, and the hydrocarbonized liquid at the top is sent to the storage tank 51 in the intermediate tank area through the de-aromatic tower 26. The hydrocarbonized liquid enters the transfer tank 27 and is transported into the benzene tower main body 31 through the second connecting pipe 28, and then flows along the conduit to the refined ethylbenzene tower 32 and then to the diethylbenzene tower 33. Benzene, refined ethylbenzene and diethylbenzene are produced in each tower in turn. For products such as ethylbenzene and polyethylbenzenes, the ethylbenzene dehydrogenation unit 4 uses the raw material ethylbenzene to flow along the ethylbenzene gas pipe 41 into the ethylbenzene dehydrogenation separation tank to form an ethylbenzene azeotrope, which is convenient for reducing the amount of water during the ethylbenzene dehydrogenation treatment. The azeotrope enters the dehydrogenation reactor 1 43 and the dehydrogenation reactor 2 44 for dehydrogenation reaction. The furnace oil after the reaction enters the distillation unit, and then the furnace oil enters the ethylene separation tower 45 and the refined styrene tower 46 in sequence. The ethylene in the tower is then sent to the tank area storage tank 2 52 for storage, which is convenient for the storage of styrene processing and production, and improves the stable production of styrene.

[0028] In the description of this utility model, it should be noted that, unless otherwise expressly specified or limited, the terms "installed," "provided with," "connected," etc., should be understood in a broad sense. For example, "connected" may refer to a fixed connection, a detachable connection, or an integral connection; it may refer to a mechanical connection or an electrical connection; it may refer to a direct connection or an indirect connection through an intermediate medium; it may refer to internal communication between two components. Those skilled in the art will be able to understand the specific meanings of the above terms in this utility model based on specific circumstances.

[0029] In the description of this embodiment, the terms "upper," "lower," "right," and other orientations or positional relationships are based on the orientations or positional relationships shown in the accompanying drawings and are intended solely for ease of description and simplified operation. They do not indicate or imply that the devices or components referred to must have a specific orientation, be constructed, or operate in a specific orientation. Therefore, they should not be construed as limitations on the present invention. Furthermore, the terms "first" and "second" are used solely for descriptive purposes and have no special meaning.

Claims

1. A styrene energy-saving production device, characterized in that: The invention comprises a device body (1), wherein the device body (1) comprises an alkylation unit (2), a distillation unit (3), an ethylbenzene dehydrogenation unit (4) and a tank area unit (5); the distillation unit (3) is arranged on the front side of the alkylation unit (2), and the ethylbenzene dehydrogenation unit (4) is arranged on one side of the alkylation unit (2); and the tank area unit (5) is respectively provided with a storage tank 1 (51) and a storage tank 2 (52).

2. A styrene energy-saving production device according to claim 1, characterized in that: The alkylation unit (2) comprises an alkylation reactor (22), a pre-fractionation tower (23) and a de-aromatization tower (26). There are two alkylation reactors (22), and an air inlet pipe (21) is provided on the outer wall of the left alkylation reactor (22). A diethylbenzene pipe (24) is provided below the air inlet pipe (21), and one end of the diethylbenzene pipe (24) is provided at the bottom of the right alkylation reactor (22).

3. A styrene energy-saving production device according to claim 2, characterized in that: The upper end of the alkylation reactor (22) is provided with a first connecting pipe (25), and one end of the first connecting pipe (25) is connected to the pre-fractionation tower (23). A de-aromatic tower (26) is provided on one side of the pre-fractionation tower (23). The bottom of the pre-fractionation tower (23) is connected to the inside of a transport tank (27), and a second connecting pipe (28) is provided on the outer wall of the transport tank (27).

4. The styrene energy-saving production device according to claim 3, characterized in that: One end of the second connecting pipe (28) is connected to the inside of the benzene tower body (31); a refined ethylbenzene tower (32) is provided on one side of the benzene tower body (31); and a diethylbenzene tower (33) is provided on one side of the refined ethylbenzene tower (32); an air outlet pipe (34) is provided on the outer wall of the diethylbenzene tower (33); and one end of the air outlet pipe (34) is connected to the storage tank (51).

5. The styrene energy-saving production device according to claim 1, characterized in that: The ethylbenzene dehydrogenation unit (4) comprises an ethylbenzene gas pipe (41), one end of which is connected to the interior of an ethylbenzene steam separation tank (42). A dehydrogenation reactor 1 (43) is provided in front of the ethylbenzene steam separation tank (42), and a dehydrogenation reactor 2 (44) is provided in front of the dehydrogenation reactor 1 (43).

6. The styrene energy-saving production device according to claim 5, characterized in that: The outer wall of the second dehydrogenation reactor (44) is provided with a connecting pipe, and one end of the connecting pipe is connected to the ethylene separation tower (45). A refined styrene tower (46) is provided on one side of the ethylene separation tower (45).

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