Industrial C10 crude aromatic hydrocarbon production device

Abstract

The utility model relates to the technical field of chemical production, and particularly discloses an industrial C10 crude aromatic hydrocarbon production device. The device comprises a refining tower and a heavy component removal tower, a tower bottom outlet of the refining tower is provided with a first pipeline, the first pipeline is provided with a first branch of the first pipeline and a second branch of the first pipeline, and the first branch of the first pipeline is connected to a side inlet of a tower body of the heavy component removal tower; an SA-1500 product outlet pipeline is arranged at the top of the heavy component removal tower, and a C10 crude aromatic hydrocarbon outlet pipeline is arranged at the bottom of the heavy component removal tower; a second branch of the first pipeline is connected to a C10 crude aromatic hydrocarbon outlet pipeline; and a first flow regulating valve and a second flow regulating valve are respectively arranged on the first branch of the first pipeline and the second branch of the first pipeline. According to the utility model, by changing the process flow of the de-heavy tower and adjusting the flow direction of materials at the top and the bottom of the de-heavy tower, the production load of the de-heavy tower is reduced so as to produce qualified industrial C10 crude aromatic hydrocarbon products, and the steam heat source amount is reduced so as to achieve economic balance.

Description

Technical Field

[0001] The utility model relates to the technical field of chemical production, and specifically discloses an industrial C10 crude aromatics production device. Background Art

[0002] With the country's regulation of the solvent market, high-boiling-point aromatic solvent SA-2000 is subject to consumption tax, and the profit of high-boiling-point aromatic solvent SA-2000 products has declined. In the market, industrial C10 crude aromatics products have a large market demand and high product prices compared to high-boiling-point aromatic solvent SA-2000.

[0003] The heavy aromatics separation unit produces four products: high-boiling-point solvent SA-1000, 1,2,4-trimethylbenzene, high-boiling-point aromatic solvent SA-1500, and high-boiling-point aromatic solvent SA-2000. The process utilizes a three-tower continuous distillation process. The heavy aromatics feedstock enters the lightness removal column, where distillation produces the high-boiling-point solvent SA-1000 at the top. The bottoms of the lightness removal column enter the refining column, where distillation produces 1,2,4-trimethylbenzene at the top. The bottoms of the refining column enter the heavy removal column, where distillation produces the high-boiling-point aromatic solvent SA-1500 at the top and the high-boiling-point aromatic solvent SA-2000 at the bottom.

[0004] The de-weighting tower is mainly used to separate SA-1500 products and SA-2000 products. SA-1500 products are distilled out at the top of the de-weighting tower as light components, and SA-2000 products are distilled out at the bottom of the de-weighting tower as heavy components.

[0005] Because the separation efficiency of the de-weighting tower equipment is already established, process adjustments can only be made to increase the light component content in the de-weighting tower bottoms to meet the industrial C10 crude aromatics product requirement of at least 30% recovery volume at 210°C. A common approach is to maintain the steam flow at the bottoms of the de-weighting tower, significantly reduce the SA-1500 product overhead, and increase the de-weighting tower reflux rate to suppress the light components at the bottoms, while ensuring the acceptable recovery volume of the industrial C10 crude aromatics product at the bottoms of the de-weighting tower. This is uneconomical due to the significant loss of SA-1500 product. Alternatively, reducing the steam flow at the bottoms impairs separation efficiency, increasing the light component content at the bottoms, and achieving acceptable industrial C10 crude aromatics product, but exceeding the heavy component standard in the SA-1500 overhead product, resulting in a substandard SA-1500 product with a dry point exceeding 215°C. A subsequent separation tower is required to separate the substandard SA-1500, but this requires significant investment and is uneconomical.

[0006] Although both the top and bottom products of the deweighting tower of Method 1 are qualified, a large amount of SA-1500 product is lost and becomes the industrial C10 crude aromatics product, which is not economical. Moreover, when the industrial C10 crude aromatics product produced by this method is subjected to product distillation range analysis, sudden boiling often occurs in the stage where the heating temperature is less than 210°C, indicating that a stable industrial C10 crude aromatics product cannot be directly distilled out.

[0007] Therefore, it is necessary to provide an energy-saving technology for the production of industrial C10 crude aromatics. By changing the process flow of the de-weighting tower, adjusting the material flow direction at the top and bottom of the de-weighting tower, reducing the production load of the de-weighting tower, and producing qualified industrial C10 crude aromatics products, it can also save the steam energy consumption of the de-weighting tower unit. Utility Model Content

[0008] The technical solutions adopted in this utility model are as follows:

[0009] The utility model provides an industrial C10 crude aromatics production device, comprising a refining tower 1 and a de-weighting tower 2, wherein the bottom outlet of the refining tower 1 is provided with a first pipeline 3, the first pipeline 3 is provided with a first pipeline first branch 3-1 and a first pipeline second branch 3-2, the first pipeline first branch 3-1 is connected to the side inlet of the tower body of the de-weighting tower 2; the top of the de-weighting tower 2 is provided with an SA-1500 product outlet pipeline 5, and the bottom of the de-weighting tower 2 is provided with a C10 crude aromatics outlet pipeline 6; the first pipeline second branch 3-2 is connected to the C10 crude aromatics outlet pipeline 6; the first pipeline first branch 3-1 and the first pipeline second branch 3-2 are respectively provided with a first flow regulating valve 7-1 and a second flow regulating valve 7-2.

[0010] Preferably, a first flow meter 8-1 and a second flow meter 8-2 are respectively provided on the first branch 3-1 of the first pipeline and the second branch 3-2 of the first pipeline for measuring the flow through the branch pipelines.

[0011] Preferably, a first bottom pump 9 is provided on the first pipeline 3 at the bottom of the refining tower 1 for providing power.

[0012] Preferably, a second bottom pump 10 is provided on the C10 crude aromatics outlet pipeline 6 at the bottom of the deweighting tower 2 for providing power.

[0013] Preferably, the inlet feed of the refining tower 1 is: the bottom material of the light-removal tower after the heavy aromatics raw material is distilled through the light-removal tower.

[0014] Preferably, the top of the refining tower 1 is provided with an outlet to produce 1,2,4-trimethylbenzene.

[0015] Beneficial effects achieved by this utility model:

[0016] The utility model changes the process flow of the de-weighting tower, adjusts the flow direction of the materials at the top and bottom of the de-weighting tower, and reduces the production load of the de-weighting tower to produce qualified industrial C10 crude aromatic products; for the reduced economic value of the SA-1500 product, the production load of the de-weighting tower is reduced and the amount of steam heat source is reduced to achieve economic balance. The final heavy aromatic separation device is capable of producing industrial C10 crude aromatic products, while reducing the amount of steam and improving economic efficiency. When the flow of the first branch 3-1 of the first pipeline and the second branch 3-2 of the first pipeline are matched in a ratio of 7:3, the production load of the de-weighting tower is reduced by 5.4%; at the same time, the steam energy consumption of the de-weighting tower is reduced from 1300kg / h to 850kg / h, and the energy consumption of the de-weighting tower is reduced by 34.62%. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 This is a schematic structural diagram of an industrial C10 crude aromatics production device according to the present invention. DETAILED DESCRIPTION

[0018] In order to make the purpose, technical solution and advantages of the present invention more clear and distinct, the present invention is further described in detail in conjunction with the following embodiments. It should be noted that the present invention is not limited to the following embodiments.

[0019] Example 1

[0020] like Figure 1 As shown, an industrial C10 crude aromatics production device includes a refining tower 1 and a de-weighting tower 2. The bottom outlet of the refining tower 1 is provided with a first pipeline 3, which is provided with a first branch 3-1 of the first pipeline and a second branch 3-2 of the first pipeline. The first branch 3-1 of the first pipeline is connected to the side inlet of the de-weighting tower 2. The top of the de-weighting tower 2 is provided with an SA-1500 product outlet pipeline 5, and the bottom of the de-weighting tower 2 is provided with a C10 crude aromatics outlet pipeline 6. The second branch 3-2 of the first pipeline is connected to the C10 crude aromatics outlet pipeline 6. The first branch 3-1 and the second branch 3-2 of the first pipeline are respectively provided with a first flow regulating valve 7-1 and a second flow regulating valve 7-2. The first branch 3-1 and the second branch 3-2 of the first pipeline are respectively provided with a first flow meter 8-1 and a second flow meter 8-2 for measuring the flow through the branch pipeline. The first pipeline 3 at the bottom of the refining tower 1 is provided with a first bottom pump 9 for providing power. A second bottom pump 10 is provided on the C10 crude aromatics outlet pipe 6 at the bottom of the heavy-removal tower 2 to provide power. The inlet feed of the refining tower 1 is the bottoms of the light-removal tower after the heavy aromatics feedstock has been distilled through the light-removal tower. The top of the refining tower 1 is provided with an outlet to produce 1,2,4-trimethylbenzene.

[0021] During production, the following steps are specifically included:

[0022] The bottom material of the de-lightening tower after the heavy aromatics raw material is distilled in the de-lightening tower enters the refining tower 1, and the 1,2,4-trimethylbenzene is discharged from the top of the refining tower 1 after distillation; the material is discharged from the bottom of the refining tower 1, and the first flow regulating valve 7-1 and the second flow regulating valve 7-2 are adjusted to make the flow rate of the first branch 3-1 of the first pipeline and the second branch 3-2 of the first pipeline be 7:3; after the first branch 3-1 of the first pipeline enters the de-lightening tower 2, the SA-1500 product is output from the SA-1500 product outlet pipeline 5 at the top of the tower, and the C10 crude aromatics outlet pipeline 6 at the bottom of the tower merges with the second branch 3-2 of the first pipeline to produce C10 crude aromatics.

[0023] The new process reduces the amount of material 1 entering the de-weighting column compared to the original process, lowering the de-weighting column's production load and reducing energy consumption. Energy consumption statistics show that, for the same output of industrial C10 crude aromatics, less heat source is required to meet system process requirements, resulting in a 34.62% energy saving in the production of industrial C10 crude aromatics. The de-weighting column only needs to produce qualified SA-1500 product according to the original production process requirements. The de-weighting column bottoms and undistilled material 2 are mixed to produce the industrial C10 crude aromatics product. Flow meters and regulating valves are installed in the branch lines to control the metering of both materials, allowing for flexible adjustment of the industrial C10 crude aromatics and SA-1500 product volumes. Flexible adjustments can be made to the SA-1500 product price, the industrial C10 crude aromatics product price, and the steam price, ensuring production control in an economically efficient manner.

Claims

1. An industrial C10 crude aromatics production device, characterized in that: The invention comprises a refining tower (1) and a de-weighting tower (2); the refining tower (1) is provided with a first pipeline (3) at the bottom outlet; the first pipeline (3) is provided with a first pipeline first branch (3-1) and a first pipeline second branch (3-2); the first pipeline first branch (3-1) is connected to the side entrance of the de-weighting tower (2); the top of the de-weighting tower (2) is provided with an SA-1500 product outlet pipeline (5); the bottom of the de-weighting tower (2) is provided with a C10 crude aromatics outlet pipeline (6); the first pipeline second branch (3-2) is connected to the C10 crude aromatics outlet pipeline (6); the first pipeline first branch (3-1) and the first pipeline second branch (3-2) are respectively provided with a first flow regulating valve (7-1) and a second flow regulating valve (7-2).

2. The industrial C10 crude aromatics production device according to claim 1, characterized in that: The first branch (3-1) of the first pipeline and the second branch (3-2) of the first pipeline are respectively provided with a first flow meter (8-1) and a second flow meter (8-2) for measuring the flow through the branch pipelines.

3. The industrial C10 crude aromatics production device according to claim 1, characterized in that: A first bottom pump (9) is provided on the first pipeline (3) at the bottom of the refining tower (1).

4. The industrial C10 crude aromatics production device according to claim 1, characterized in that: A second bottom pump (10) is provided on the C10 crude aromatics outlet pipeline (6) at the bottom of the deweighting tower (2).

5. The industrial C10 crude aromatics production device according to claim 1, characterized in that: The inlet feed of the refining tower (1) is: the bottom material of the light-removing tower after the heavy aromatic hydrocarbon raw material is distilled through the light-removing tower.

6. The industrial C10 crude aromatics production device according to claim 1, characterized in that: The top of the refining tower (1) is provided with an outlet to produce 1,2,4-trimethylbenzene.

Images