Combined technique for preparing olefins by using refinery C4

A combination process, C4 technology of refinery, applied in the field of new process of producing and separating olefins, can solve the problem of low utilization rate of C4 in refinery, achieve significant industrial value, reduce production cost, and increase production rate

Active Publication Date: 2008-06-25
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] In order to solve the problem of low utilization rate of C4 in refinery, the present invention proposes a method of using C4 in refinery as ra

Method used

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  • Combined technique for preparing olefins by using refinery C4
  • Combined technique for preparing olefins by using refinery C4
  • Combined technique for preparing olefins by using refinery C4

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0043] Reference attached figure 2 , with the flow rate of 17500kg / h refinery C41 as raw material, its main composition (mass percentage) is: propane 7.3%, isobutene 14.0%, 1-butene 14.0%, cis-2-butene 16.3%, trans 20.2% -2-butene, 17.0% n-butane, 0.5-10.0% isobutane, and the balance is propylene. The carbon four in the refinery enters the pre-separation tower. The number of plates in the pre-separation tower is 130. The operating conditions are: tower top pressure 0.9MPa (absolute), tower top temperature 39.4°C, tower bottom temperature 73.7°C and reflux ratio 26.6. Light ends were withdrawn with an isobutane content (mass) of 51%. After the stream in the tower kettle is preheated to 500°C, it enters the olefin catalytic cracking reactor 10 for reaction. The amount of water vapor is 9850kg / h, and the loading capacity of the catalyst is 7 tons. The catalyst adopts the catalyst of the brand BOC-1 of Beijing Research Institute of Chemical Industry. The conditions are: tempera...

Embodiment 2

[0045] Reference attached image 3 , using the same raw material as in Example 1, enter the gas-liquid separation tank 19 after the pre-separation tower 1, olefin cracking reactor 10, oil washing tower 11, water washing tower 12, compression unit 13, and the separated gas phase goes to the absorption tower 14 , the separated liquid phase goes to the precipitation tower 20, and the separation tower still stream is sent to the debutanizer 15; the debutanizer overhead stream is sent to the depropanizer 16, and the tower still stream is partially recycled to the absorption tower, and partly extracted, The ratio is 2.8:1; the operating conditions of the above units are the same as in Example 1. The number of plates of the depropanizer is 40, the temperature at the top of the tower is 51° C., the pressure at the top of the tower is 2.0 MPa (absolute), and the reflux ratio is 2. The carbon four components extracted from the bottom of the depropanizer are sent out of the boundary are...

Embodiment 3

[0047] Adopt the raw material identical with embodiment 2, enter gas-liquid separation tank 19 after pre-separation tower 1, olefin cracking reactor 10, oil washing tower 11, water washing tower 12, compression unit 13, through absorption tower 14, separating out tower 20, Debutanizer 15; the debutanizer tower bottom stream is partially recycled to the absorption tower, and part of the extraction is 2.8:1; the debutanizer top stream is sent to the depropanizer 16, and the carbon is extracted from the depropanizer top Three component 6790kg / h, sent out of the boundary area as a product; carbon four component 8780kg / h extracted from the depropanizer tower kettle, sent out of the boundary area as a product. The operating conditions of the above units are the same as in Example 2.

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Abstract

A method for utilizing the C4 raffinate to prepare the olefin of the invention belongs to the technical field of olefin preparation. In order to solve the problem that the C4 raffinate can not be sufficiently utilized, the invention proposes that the C4 raffinate is first pre-separated so as to remove the propane, the propylene and the isobutene in the C4 raffinate and then the treated C4 raffinate is delivered to an olefin catalytic cracking system, and the generated cracking gas mixtures go into a cooling system to be cooled down and then are compressed with entering a compression section; the compressed catalytic cracking gas goes into an absorption tower and the light components such as the methane, the C2, etc. are produced from the top of the absorption tower and the column bottom matters flow through a separation system with being separated so as to respectively obtain the C3 components, the C4 components and the C5 components and heavier components with the C5 and heavier components as absorbents. The combined process of the invention has the advantages of sufficient utilization of the C4 raffinate, few hydrogen circulations, low energy consumption, high propylene yield, simple operation, low investment, etc.

Description

technical field [0001] The invention relates to a method for preparing olefins, in particular to a new process for preparing and separating olefins by adopting the methods of catalytic cracking of olefins, oil absorption and extractive distillation. Background technique [0002] With the improvement of my country's crude oil processing capacity, the catalytic cracking unit of the refinery will by-produce a large amount of C4 hydrocarbons. The production of ethylene and propylene from a large number of surplus and cheap C4 hydrocarbons is an important way to combine oil and chemical industry and efficiently utilize C4 resources, which can bring significant economic benefits to petrochemical enterprises. Around the comprehensive utilization of C4 in refineries, major companies and research institutes at home and abroad have carried out a lot of research and made some progress, but few of them have achieved industrial applications. [0003] ABB Lummus Global's OCT process uses...

Claims

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Application Information

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IPC IPC(8): C07C4/06C07C11/04C07C11/06B01J29/076
CPCY02P20/52Y02P30/40
Inventor 张勇程建民戴伟李东风刘智信王定博陈硕刘小波
Owner CHINA PETROLEUM & CHEM CORP
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