Preparation system of high-purity 2, 4, 4-trimethyl-1-pentene and 2, 4, 4-trimethyl-2-pentene

Abstract

The utility model discloses a preparation system of high-purity 2, 4, 4-trimethyl-1-pentene and 2, 4, 4-trimethyl-2-pentene, which comprises the following steps: by taking crude diisobutylene as a raw material, firstly carrying out light component removal and heavy component removal rectification separation to obtain diisobutylene, and then carrying out extractive distillation, solvent recovery and separation to obtain high-purity 2, 4, 4-trimethyl-1-pentene and 2, 4, 4-trimethyl-2-pentene. The utility model relates to a 2, 4, 4-trimethyl-1-pentene and 2, 4, 4-trimethyl-2-pentene product. The method has the advantages of short process flow, high product purity, wide solvent application range and the like.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the technical field of petroleum chemical industry, especially relates to a kind of preparation system of high purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene. BACKGROUND

[0002] Diisobutylene is an important organic intermediate, widely used in synthetic rubber tackifier, surfactant and octylphenol, isononyl alcohol and other fields.

[0003] In the industrial field, 2,4,4-trimethyl-2-pentene is usually mixed with 2,4,4-trimethyl-1-pentene, and sold as a mixture of diisobutylene. However, in downstream applications, although both components can participate in the reaction, 2,4,4-trimethyl-2-pentene usually needs to be isomerized to 2,4,4-trimethyl-1-pentene before participating in the reaction, which directly affects the reaction speed and production efficiency. To improve the utilization rate and economy of components, efficient separation of the two isomers is necessary.

[0004] CN109867583A discloses a process for obtaining 2,4,4-trimethyl-1-pentene from carbon four polymerization oil and its system device, but the method process separates the extractant from the heavy component after extractive distillation, which has the problems of high energy consumption and small application range of extractant.

[0005] CN108056576A discloses a preparation method of 2,4,4-trimethyl-1-pentene, which does not need to be distilled and refined, but has the problems of long reaction time, high requirement for reaction equipment material, and high difficulty in industrialization. UTILITY MODEL CONTENT

[0006] Therefore, the utility model aims to provide a preparation system of high purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene to solve at least one technical problem in the background art.

[0007] To achieve the above-mentioned purpose, the technical scheme of the utility model is as follows:

[0008] A preparation system of high purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene, comprising a light removal column, a heavy removal column reboiler, an extractive distillation column and a solvent recovery column connected in sequence;

[0009] The raw material enters from one side of the light removal column, and the light component is discharged from the top of the light removal column, and the C8+ component is discharged from the bottom of the heavy removal column reboiler;

[0010] 2,4,4-trimethyl-1-pentene product is taken out from the top of the extractive distillation column;

[0011] The overhead of the solvent recovery column is taken out 2,4,4-trimethyl-2-pentene product.

[0012] Further, the bottom of the light-removing column is communicated with the middle part of the heavy-removing column, the overhead of the heavy-removing column is communicated with the lower part of the extractive rectification column, the bottom of the extractive rectification column is communicated with the middle part of the solvent recovery column, and the bottom of the solvent recovery column is communicated with the upper part of the extractive rectification column.

[0013] Further, the bottom of the light-removing column is provided with a first branch and a second branch, the first branch is communicated with the middle part of the heavy-removing column, the second branch is communicated with the bottom of the light-removing column reboiler, and the second branch is provided with a light-removing column reboiler;

[0014] The overhead of the light-removing column is communicated with a light-removing column cooler through a pipeline, the light-removing column cooler is provided with a third branch and a fourth branch, the third branch is used for taking out light components, and the fourth branch is communicated with the upper part of the light-removing column.

[0015] Further, the overhead of the heavy-removing column is communicated with a heavy-removing column cooler through a pipeline, the heavy-removing column cooler is connected with a fifth branch and a sixth branch, the fifth branch is communicated with the middle part of the extractive rectification column, and the sixth branch is communicated with the upper part of the heavy-removing column;

[0016] The bottom of the heavy-removing column is provided with a seventh branch and an eighth branch, the seventh branch is connected with the middle part of the heavy-removing column, the seventh branch is provided with a heavy-removing column reboiler, and the eighth branch is used for taking out C8+ components.

[0017] Further, the bottom of the extractive rectification column is provided with a ninth branch and a tenth branch, the ninth branch is communicated with the middle part of the solvent recovery column,

[0018] the tenth branch is communicated with the lower part of the extractive rectification column;

[0019] the tenth branch is provided with an extractive rectification column reboiler;

[0020] The overhead of the extractive rectification column is connected with an extractive rectification column cooler through a pipeline, the extractive rectification column cooler is provided with an eleventh branch and a twelfth branch,

[0021] the eleventh branch is communicated with the upper part of the extractive rectification column, and the twelfth branch is used for taking out 2,4,4-trimethyl-1-pentene product.

[0022] Further, the overhead of the solvent recovery column is connected with a solvent recovery column cooler through a pipeline, the solvent recovery column cooler is provided with a thirteenth branch and a fourteenth branch, the thirteenth branch is connected with the upper part of the solvent recovery column, and the fourteenth branch is used for taking out 2,4,4-trimethyl-2-pentene product;

[0023] Further, the solvent recovery column is provided with a fifteenth branch and a sixteenth branch, the fifteenth branch is communicated with the lower part of the solvent recovery column, the fifteenth branch is provided with a solvent recovery column reboiler, and the sixteenth branch is communicated with the upper part of the extractive rectification column.

[0024] Compared with the prior art, the preparation system of high-purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene has the following advantages:

[0025] The preparation system is reasonably arranged, and the isomers of diisobutylene can be separated at low energy consumption to obtain high-purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene products;

[0026] 2. The preparation system is widely applicable and friendly to composite extractants, and provides a basis for the diversification of extractive rectification extractants. BRIEF DESCRIPTION OF DRAWINGS

[0027] The accompanying drawings, which form a part of this application, are included to provide a further understanding of the application and are incorporated herein for illustration only. The embodiments of the present application and the description thereof are presented for the purpose of exemplification and by way of interpretation of the present application, but are not meant as an inappropriate limitation on the present application. In the drawings:

[0028] Figure 1 A preparation system of high-purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene according to the present application is shown in the accompanying drawings.

[0029] LEGEND OF THE DRAWINGS

[0030] 1. Light removal column; 2. Light removal column reboiler; 3. Light removal column cooler; 4. Heavy removal column cooler; 5. Heavy removal column; 6. Heavy removal column reboiler; 7. Extractive rectification column cooler; 8. Extractive rectification column; 9. Extractive rectification column reboiler; 10. Solvent recovery column cooler; 11. Solvent recovery column; 12. Solvent recovery column reboiler. DETAILED DESCRIPTION

[0031] It should be noted that the embodiments in the present application and the features in the embodiments can be combined with each other without conflict.

[0032] In the description of this utility model, it should be understood that the terms "center," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicating orientation or positional relationships based on the orientation or positional relationships shown in the accompanying drawings, are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, features defined with "first," "second," etc., may explicitly or implicitly include one or more of that feature. In the description of this utility model, unless otherwise stated, "a plurality of" means two or more.

[0033] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0034] The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0035] like Figure 1 As shown, a method for preparing high-purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene includes the following steps: using crude diisobutylene as raw material, firstly, diisobutylene is obtained by separation through light and heavy component removal distillation; then, high-purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene products are obtained by extraction distillation and solvent recovery. The crude diisobutylene, by mass, comprises: 1%-15% light component, 37%-58% 2,4,4-trimethyl-1-pentene, 8%-20% 2,4,4-trimethyl-2-pentene, and 7%-40% C8+ component.

[0036] The extractant used in extractive distillation includes one or more of N,N-dimethylformyl, N,N-diethylaniline, and triethanol.

[0037] Light weight removal is carried out in light weight removal tower 1. The top temperature of light weight removal tower 1 is 80-90℃, the top pressure is 0.05-0.15MPaG, the bottom temperature is 140-160℃, and the bottom pressure is 0.10-0.14MPaG.

[0038] The de-heavy separation is carried out in the de-heavy tower 5, the tower top temperature of the de-heavy tower 5 is 50-60℃, the tower top pressure is -0.6--0.8MpaG, the tower bottom temperature is 140-160℃, and the tower bottom pressure is -0.05--0.07MPaG;

[0039] The extractive distillation is carried out in the extractive distillation tower 8, the tower top temperature of the extractive distillation tower 8 is 55-60℃, the tower top pressure is -0.08--0.10MPaG, the tower bottom temperature is 110-120℃, and the tower bottom pressure is -0.06--0.12MPaG;

[0040] The solvent recovery is carried out in the solvent recovery tower 11, the tower top temperature of the solvent recovery tower 11 is 50-70℃, the tower top pressure is -0.06--0.08MPaG, the tower bottom temperature is 110-130℃, and the tower bottom pressure is -0.07--0.09MPaG.

[0041] The preparation system used in the above-mentioned method for preparing high-purity 2,4,4-trimethyl-1-pentene and 2,4,4-trimethyl-2-pentene comprises a de-light tower 1, a de-heavy tower reboiler 6, an extractive distillation tower 8 and a solvent recovery tower 11 connected in sequence; the raw material enters from one side of the de-light tower 1, the light components are discharged from the tower top of the de-light tower 1, and the C8+ components are discharged from the tower bottom of the de-heavy tower reboiler 6; the 2,4,4-trimethyl-1-pentene product is taken out from the tower top of the extractive distillation tower 8; and the 2,4,4-trimethyl-2-pentene product is taken out from the tower top of the solvent recovery tower 11.

[0042] The tower bottom of the de-light tower 1 is communicated with the middle part of the de-heavy tower 5, the tower top of the de-heavy tower 5 is communicated with the lower part of the extractive distillation tower 8, the tower bottom of the extractive distillation tower 8 is communicated with the middle part of the solvent recovery tower 11, and the tower bottom of the solvent recovery tower 11 is communicated with the upper part of the extractive distillation tower 8. The tower bottom of the de-light tower 1 is provided with a first branch and a second branch, the first branch is communicated with the middle part of the de-heavy tower 5, the second branch is communicated with the bottom of the de-light tower reboiler 2, and the de-light tower reboiler 2 is arranged on the second branch; the tower top of the de-light tower 1 is communicated with the de-light tower cooler 3 through a pipeline, the de-light tower cooler 3 is provided with a third branch and a fourth branch, the third branch is used for taking out the light components, and the fourth branch is communicated with the upper part of the de-light tower 1.

[0043] The tower top of the de-heavy tower 5 is communicated with the de-heavy tower cooler 4 through a pipeline, the de-heavy tower cooler 4 is connected with a fifth branch and a sixth branch, the fifth branch is communicated with the middle part of the extractive distillation tower 8, and the sixth branch is communicated with the upper part of the de-heavy tower 5; the tower bottom of the de-heavy tower 5 is provided with a seventh branch and an eighth branch, the seventh branch is connected with the middle part of the de-heavy tower 5, the de-heavy tower reboiler 6 is arranged on the seventh branch, and the eighth branch is used for taking out the C8+ components.

[0044] The bottom of the extractive distillation column 8 is provided with a ninth branch and a tenth branch, the ninth branch is communicated with the middle part of the solvent recovery column 11, and the tenth branch is communicated with the lower part of the extractive distillation column 8; the tenth branch is provided with an extractive distillation column reboiler 9; the top of the extractive distillation column 8 is connected with an extractive distillation column cooler 7 through a pipeline, and the extractive distillation column cooler 7 is provided with an eleventh branch and a twelfth branch, the eleventh branch is communicated with the upper part of the extractive distillation column 8, and the twelfth branch is used to extract 2,4,4-trimethyl-1-pentene product.

[0045] The top of the solvent recovery column 11 is connected with a solvent recovery column cooler 10 through a pipeline, the solvent recovery column cooler 10 is provided with a thirteenth branch and a fourteenth branch, the thirteenth branch is connected with the upper part of the solvent recovery column 11, and the fourteenth branch is used to extract 2,4,4-trimethyl-2-pentene product; the bottom of the solvent recovery column 11 is provided with a fifteenth branch and a sixteenth branch, the fifteenth branch is communicated with the lower part of the solvent recovery column 11, the fifteenth branch is provided with a solvent recovery column reboiler 12, and the sixteenth branch is communicated with the upper part of the extractive distillation column 8.

[0046] Example 1

[0047] In the specific implementation, the crude diisobutene composition is 8.5% of light components, 45.2% of 2,4,4-trimethyl-1-pentene, 11.3% of 2,2,4-trimethyl-2-pentene, and 35% of C8+ component isobutane, the crude diisobutene enters the light removal column 1, the top temperature is 85°C, the top pressure is 0.1 MPaG, the bottom temperature is 150°C, and the bottom pressure is 0.12 MPaG, the light components are extracted from the top, and the components after light removal are extracted from the bottom and enter the heavy removal column 5, the top temperature of the heavy removal column 5 is 55°C, the top pressure is-0.7 MPaG, the bottom temperature is 150°C, and the bottom pressure is-0.06 MPaG, and the C8+ components are extracted from the bottom; the C8+ components after heavy removal are extracted from the top of the heavy removal column 5 and enter the extractive distillation column 8 through the lower part of the extractive distillation column 8; N,N-dimethylformamide is selected as the extractant and enters the extractive distillation column 8 through the upper part of the extractive distillation column 8, the mass ratio of the solvent to the C8+ components is 3:1, the top temperature of the extractive distillation column 8 is 55°C, the top pressure is-0.09 MPaG, the bottom temperature is 115°C, and the bottom pressure is-0.08 MPaG, after extractive distillation, the 2,4,4-trimethyl-1-pentene product is extracted from the top, and the product purity is 97.1%; the solvent rich in 2,4,4-trimethyl-2-pentene enters the solvent recovery column 11 from the bottom of the extractive distillation column 8, the top temperature of the solvent recovery column 11 is 60°C, the top pressure is-0.07 MPaG, the bottom temperature is 120°C, and the bottom pressure is-0.08 MPaG, the 2,4,4-trimethyl-2-pentene with a purity of 96.7% is extracted from the top of the solvent recovery column 11, the recovered solvent is extracted from the bottom and returned to the extractive distillation column 8 for recycling.

[0048] Example 2

[0049] The difference from Example 1 is that the solvent composition is 85 wt% N,N- dimethylacetamide, 13 w% N,N-diethylaniline, 2 wt% triethanolamine mixture, and the product 2,4,4-trimethyl-1-pentene is obtained with a purity of 98.5%, and 2,4,4-trimethyl-2-pentene with a purity of 99.3%.

[0050] Example 3

[0051] The difference from Example 1 is that the solvent composition is 85 wt% N,N- dimethylacetamide and 15 w% N,N-diethylaniline;

[0052] The product 2,4,4-trimethyl-1-pentene is obtained with a purity of 97.5%, and 2,4,4-trimethyl-2-pentene with a purity of 97.3%.

[0053] Example 4

[0054] The difference from Example 1 is that the solvent composition is 75 wt% N,N- dimethylacetamide and 25 w% triethanolamine;

[0055] The product 2,4,4-trimethyl-1-pentene is obtained with a purity of 97.8%, and 2,4,4-trimethyl-2-pentene with a purity of 97.9%.

[0056] Example 5

[0057] The difference from Example 1 is that the solvent composition is triethanolamine; the product 2,4,4-trimethyl-1-pentene is obtained with a purity of 90.5%, and 2,4,4-trimethyl-2-pentene with a purity of 85.3%.

[0058] Example 6

[0059] In a specific implementation, the crude diisobutylene composition is 8.5% light components, 45.2% 2,4,4-trimethyl-1-pentene, 11.3% 2,2,4-trimethyl-2-pentene, 35% C8+ components. The crude diisobutylene enters the light-removing column 1, the overhead temperature is 85°C, the overhead pressure is 0.1 MPaG, the column bottom temperature is 150°C, the column bottom pressure is 0.12 MPaG, the light components are taken out from the overhead, and the light-removed components are taken out from the column bottom to enter the heavy-removing column 5. The overhead temperature of the heavy-removing column 5 is 55°C, the overhead pressure is -0.7 MPaG, the column bottom temperature is 150°C, the column bottom pressure is -0.06 MPaG, and the C8+ components are taken out from the column bottom. The C8+ components after heavy-removing are taken out from the overhead of the heavy-removing column 5 and enter the extractive rectification column 8 from the lower part of the extractive rectification column 8. N-formamide is selected as the extractant, which enters the extractive rectification column 8 from the upper part of the extractive rectification column 8, and the mass ratio of the solvent to the C8+ components is 4:1. The overhead temperature of the extractive rectification column 8 is 57°C, the overhead pressure is -0.08 MPaG, the column bottom temperature is 118°C, and the column bottom pressure is -0.07 MPaG. After extractive rectification, the 2,4,4-trimethyl-1-pentene product is taken out from the overhead, and the product purity is 96.1%. The solvent rich in 2,4,4-trimethyl-2-pentene enters the solvent recovery column 11 from the column bottom of the extractive rectification column 8. The overhead temperature of the solvent recovery column 11 is 60°C, the overhead pressure is -0.07 MPaG, the column bottom temperature is 120°C, and the column bottom pressure is -0.08 MPaG. The 2,4,4-trimethyl-2-pentene with a purity of 95.7% is taken out from the overhead of the solvent recovery column 11, and the recovered solvent is taken out from the column bottom to return to the extractive rectification column 8 for recycling

[0060] Example 7

[0061] In a specific implementation, the crude diisobutene composition is 8.5% light components, 45.2% 2,4,4-trimethyl-1-pentene, 11.3% 2,2,4-trimethyl-2-pentene, 35% C8+ component isobutane, the crude diisobutene enters the light removal column 1, the column top temperature is 85℃, the column top pressure is 0.1MPaG, the column bottom temperature is 150℃, the column bottom pressure is 0.12MpaG, the light components are taken out from the column top, the components after light removal are taken out from the column bottom and enter the heavy removal column 5, the column top temperature of the heavy removal column 5 is 55℃, the column top pressure is -0.7MpaG, the column bottom temperature is 150℃, the column bottom pressure is -0.06MPaG, the C8+ components are taken out from the column bottom; the C8+ components after heavy removal are taken out from the column top of the heavy removal column 5, enter the extractive distillation column 8 through the lower part of the extractive distillation column 8, the sulfolane is selected as the extractant, enters the extractive distillation column 8 through the upper part of the extractive distillation column 8, the mass ratio of the solvent and the C8+ components is 6:1, the column top temperature of the extractive distillation column 8 is 55℃, the column top pressure is -0.09MPaG, the column bottom temperature is 115℃, the column bottom pressure is -0.08MPaG, after extractive distillation, the 2,4,4-trimethyl-1-pentene product is taken out from the column top, the product purity is 92.7%; the solvent rich in 2,4,4-trimethyl-2-pentene enters the solvent recovery column 11 from the column bottom of the extractive distillation column 8, the column top temperature of the solvent recovery column 11 is 60℃, the column top pressure is -0.07MPaG, the column bottom temperature is 120℃, the column bottom pressure is -0.08MPaG, the 2,4,4-trimethyl-2-pentene with a purity of 91.7% is taken out from the column top of the solvent recovery column 11, the recovered solvent is taken out from the column bottom and returned to the extractive distillation column 8 for recycling

[0062] The above merely describes the preferred embodiments of the present application and is not intended to limit the present application, and any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. A system for the preparation of high purity 2,4,4-trimethyl-l-pentene and 2,4,4-trimethyl-2-pentene, characterized by: The light-removing column, the heavy-removing column reboiler, the extractive rectification column and the solvent recovery column are sequentially connected. The raw material enters from one side of the light-removing column, the light component is discharged from the top of the light-removing column, and the C8+ component is discharged from the bottom of the heavy-removing column reboiler. The 2,4,4-trimethyl-1-pentene product is taken from the top of the extractive rectification column. The 2,4,4-trimethyl-2-pentene product is taken from the top of the solvent recovery column.

2. The system for preparing according to claim 1, characterized in that: The bottom of the light-removing column is communicated with the middle part of the heavy-removing column, the top of the heavy-removing column is communicated with the lower part of the extractive rectification column, the bottom of the extractive rectification column is communicated with the middle part of the solvent recovery column, and the bottom of the solvent recovery column is communicated with the upper part of the extractive rectification column.

3. The system for preparing according to claim 1, characterized in that: The bottom of the light-removing column is provided with a first branch and a second branch, the first branch is communicated with the middle part of the heavy-removing column, the second branch is communicated with the bottom of the light-removing column reboiler, and the second branch is provided with the light-removing column reboiler. The top of the light-removing column is communicated with the light-removing column cooler through a pipeline, the light-removing column cooler is provided with a third branch and a fourth branch, the third branch is used for taking the light component, and the fourth branch is communicated with the upper part of the light-removing column.

4. The system for preparing according to claim 1, characterized in that: The top of the heavy-removing column is communicated with the heavy-removing column cooler through a pipeline, the heavy-removing column cooler is connected with a fifth branch and a sixth branch, the fifth branch is communicated with the middle part of the extractive rectification column, and the sixth branch is communicated with the upper part of the heavy-removing column. The bottom of the heavy-removing column is provided with a seventh branch and an eighth branch, the seventh branch is connected with the middle part of the heavy-removing column, the seventh branch is provided with the heavy-removing column reboiler, and the eighth branch is used for taking the C8+ component.

5. The system for preparing according to claim 1, characterized in that: The bottom of the extractive rectification column is provided with a ninth branch and a tenth branch, the ninth branch is communicated with the middle part of the solvent recovery column, the tenth branch is communicated with the lower part of the extractive rectification column, the tenth branch is provided with the extractive rectification column reboiler, the top of the extractive rectification column is connected with the extractive rectification column cooler through a pipeline, the extractive rectification column cooler is provided with an eleventh branch and a twelfth branch, the eleventh branch is communicated with the upper part of the extractive rectification column, and the twelfth branch is used for taking the 2,4,4-trimethyl-1-pentene product.

6. The system for preparing according to claim 1, characterized in that: The top of the solvent recovery column is connected with the solvent recovery column cooler through a pipeline, the solvent recovery column cooler is provided with a thirteenth branch and a fourteenth branch, the thirteenth branch is connected with the upper part of the solvent recovery column, and the fourteenth branch is used for taking the 2,4,4-trimethyl-2-pentene product.

7. The system for producing according to claim 6, characterized in that: The bottom of the solvent recovery column is provided with a fifteenth branch and a sixteenth branch, the fifteenth branch is communicated with the lower part of the solvent recovery column, the fifteenth branch is provided with the solvent recovery column reboiler, and the sixteenth branch is communicated with the upper part of the extractive rectification column.

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