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Separating and purifying device and process for heavy-component residual liquid of hydrogenation process of coking crude benzene

A technology for coking crude benzene and heavy components, applied in the field of rectification, can solve problems such as waste of resources, and achieve the effects of less investment in equipment, high separation efficiency, and good economic and social benefits

Active Publication Date: 2011-03-02
XINGTAI RISUN COAL CHEM IND
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In the early days, all enterprises treated the above-mentioned heavy component raffinate as cheap solvent oil, resulting in a great waste of resources

Method used

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  • Separating and purifying device and process for heavy-component residual liquid of hydrogenation process of coking crude benzene
  • Separating and purifying device and process for heavy-component residual liquid of hydrogenation process of coking crude benzene
  • Separating and purifying device and process for heavy-component residual liquid of hydrogenation process of coking crude benzene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0022] In this example, the heavy component raffinate of the coking crude benzene hydrogenation process provided by a certain enterprise is taken as an example to illustrate the operation steps of the above-mentioned separation and purification device.

[0023] The composition of the heavy component raffinate in the coking crude benzene hydrogenation process is shown in Table 1.

[0024] Table 1 Components and contents of heavy component raffinate in coking crude benzene hydrogenation process

[0025]

[0026] Take 1.5L of the heavy component raffinate of the above-mentioned coking crude benzene hydrogenation process. The batch rectification tower is φ30mm×4000mm, the tower is filled with high-efficiency wire mesh packing, and the tower kettle is 2.0L. The process conditions for batch distillation are:

[0027] ①The total reflux operation is carried out at 40.0kPa operating pressure for about 1 hour, the temperature at the top of the tower is 60.0°C and after the pressure...

Embodiment 2

[0032] Take 1.6L of the heavy component raffinate of the coking crude benzene hydrogenation process of an enterprise, its composition and the batch rectification device adopted are the same as those described in Implementation 1. Batch distillation operation process:

[0033] ① Carry out total reflux operation at an operating pressure of 50.0kPa for about 1 hour, the temperature at the top of the tower is 65.0°C and after the pressure of the whole tower is stabilized, the light component product is extracted from the top of the tower with a reflux ratio of 3:1;

[0034] ②After the extraction of light components is completed, under the operating pressure of 15.0kPa, the temperature at the top of the tower is 120.0°C and the whole tower is stable, and the indane product is extracted from the top of the tower with a reflux ratio of 5:1;

[0035] ③After indane extraction is completed, under the operating pressure of 15.0kPa, the temperature at the top of the tower is 130°C and the...

Embodiment 3

[0038] Take 1.7L of the heavy component raffinate of the double coking crude benzene hydrogenation process of a certain enterprise, and its composition and the vacuum intermittent rectification device used are the same as those described in implementation 1. Batch distillation operation process:

[0039] ①The total reflux operation is carried out at 45.0KPa operating pressure for about 1 hour, the temperature at the top of the tower is 62.0°C and after the pressure of the whole tower is stabilized, the light component product is extracted from the top of the tower with a reflux ratio of 2:1;

[0040] ② After the extraction of light components is completed, under the operating pressure of 12.0kPa, the temperature at the top of the tower is 118.0°C and the whole tower is stable, and the indane product is extracted from the top of the tower with a reflux ratio of 4:1;

[0041] ③After indane extraction is completed, under the operating pressure of 13.0kPa, the temperature at the t...

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Abstract

The invention discloses a separating and purifying device and process for heavy component residual liquid of a hydrogenation process of coking crude benzene, belonging to the technical field of fractioning separation. The separating and purifying device of the invention comprises a tower kettle, a batch fractioning tower, a tower top fraction storage tank and a vacuum pump, wherein the batch fractioning tower is connected with the tower kettle; a condenser is arranged at the tower top of the batch fractionating tower; and the vacuum pump is respectively connected with the condenser and the tower top fraction storage tank through a buffer tank. The process comprises the following steps: when the tower top pressure is 10.0-15.0kPa, and the tower top temperature is 115.0-120.0 DEG C, collecting indan from the tower top by a reflux ratio of 4-5; after the indan is collected, when the tower top pressure is 10.0-15.0kPa, and the tower top temperature is 125.0-130.0 DEG C, collecting tetraline from the tower top by the reflux ratio of 8-10; and finally when the tower top pressure is 10.0-15.0kPa, and the tower top temperature is 155.0-160.0 DEG C, collecting naphthalene from the tower top by a reflux ratio of 4-5. The purity of the indan is 99.0wt%, the purity of the tetraline is 99.5wt%, and the purity of the naphthalene is 98.0wt%.

Description

technical field [0001] The invention relates to the technical field of rectification, in particular to a separation device and process for purifying heavy component raffinate produced in coking crude benzene hydrogenation process by adopting vacuum batch rectification. Background technique [0002] Coking crude benzene is a by-product produced in the coal coking process, rich in important compounds such as benzene, toluene and xylene (triphenyl for short), and is an important source of benzene. Due to the continuous rise of oil prices, the rapid development of my country's economy, and the increasing demand for triphenyl and its downstream products, it is obvious that the current production capacity of benzene from oil can no longer meet domestic demand. Since my country has become a major coke producer in the world and its production capacity accounts for about 60% of the world's total coke production, recovery of triphenyl and downstream products from coal coking by-produc...

Claims

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Application Information

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IPC IPC(8): B01D3/10C07C13/465C07C13/48C07C15/24C07C7/04
Inventor 张英伟华超杨洪庆夏淑倩耿瑞增高忠超罗帅许东辉
Owner XINGTAI RISUN COAL CHEM IND
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