C3 fraction liquid phase selective hydrogenation method

A technology for selective hydrogenation and fractionation, applied in the direction of hydrocarbons, chemical instruments and methods, purification/separation of hydrocarbons, etc., can solve the problems of ineffective removal and high energy consumption in the hydrogenation process, and achieve simplified C3 fractionation Liquid-phase selective hydrogenation process, reducing reaction energy consumption and improving removal effect

Active Publication Date: 2017-05-03
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] Aiming at the defect that the liquid phase selective hydrogenation method of the C3 fraction in the prior art cannot effectively remove propyne and / or propadiene in the C3 fraction, the liquid phase selective hydrogenation process of the C3 fraction is complex and consumes a lot of energy. The invention provides a new method for liquid-phase selective hydrogenation of carbon three fractions

Method used

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  • C3 fraction liquid phase selective hydrogenation method
  • C3 fraction liquid phase selective hydrogenation method

Examples

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Effect test

Embodiment 1

[0063] according to figure 1 The flow process of the carbon three liquid phase selective hydrogenation shown in the present invention.

[0064] The material f1 extracted from the top of the depropanizer S0 obtained by reacting the C3 material f0 in the depropanizer S0 passes through the water dryer S2 and the dearsenic reactor R2 sequentially through the pump S1.

[0065] The fresh C3 fraction a (flow rate is 180t / h, the sum of the molar content of propyne and propadiene is 3%) and the circulating C3 stream b (flow rate is 90t / h) extracted from the dearsenic reactor R2 After mixing, mix with hydrogen c (hydrogen flow rate is 380kg / h, hydrogen purity is 95%, other impurity is methane) after S3 heat exchange, obtained mixture d enters reactor from the top of selective hydrogenation reactor, from above Down through the selective hydrogenation catalyst bed R1 in the selective hydrogenation reactor, it is in contact with the carbon three liquid phase selective hydrogenation cataly...

Embodiment 2

[0074] According to the method described in embodiment 1, the difference is that the flow rate of the fresh carbon three fraction a is 210t / h, the flow rate of the circulating carbon three stream b is 100t / h, and the flow rate of the gas phase stream g is 110t / h, correspondingly, by Adjust the flow rate of the gaseous phase stream g entering the propylene rectification tower to adjust the pressure of the selective hydrogenation reactor to 2.35MPa.

[0075] By adopting the method provided in this example, the molar content of propyne and propadiene in the gas phase stream g obtained after gas-liquid separation is less than 200ppm.

Embodiment 3

[0077] according to figure 1 The flow process of the carbon three liquid phase selective hydrogenation shown in the present invention.

[0078] The material f1 extracted from the top of the depropanizer S0 obtained by reacting the C3 material f0 in the depropanizer S0 passes through the water dryer S2 and the dearsenic reactor R2 sequentially through the pump S1.

[0079] The fresh C3 fraction a (flow rate is 150t / h, the sum of the molar content of propyne and propadiene is 2.5%) and the circulating C3 stream b (flow rate is 75t / h) extracted from the dearsenic reactor R2 After mixing, mix with hydrogen c (hydrogen flow rate is 290kg / h, hydrogen purity is 95%, other impurity is methane) after S3 heat exchange, obtained mixture d enters reactor from the top of selective hydrogenation reactor, from above Down through the selective hydrogenation catalyst bed R1 in the selective hydrogenation reactor, it is in contact with the carbon three liquid phase selective hydrogenation cata...

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Abstract

The invention discloses a C3 fraction liquid phase selective hydrogenation method, wherein the method comprises the steps: mixing propargyl and / or allene-containing fresh C3 fraction a extracted from a depropanization tower in a propylene production process, a circular C3 material flow b and hydrogen gas c, then making the mixture contact with a selective hydrogenation catalyst, and carrying out selective hydrogenation; carrying out gas-liquid separation of the material obtained from the selective hydrogenation to obtain a gas phase material flow g containing propylene and propane and a liquid phase material flow h containing propylene and propane; dividing the liquid phase material flow h containing propylene and propane into a first part material flow i and a second part material flow j, and taking the first part material flow i as the circular C3 material flow b; and allowing the second part material flow j to return to the depropanization tower. The method provided by the invention not only effectively removes acetylene and / or allene in the C3 fraction but also reduces the energy consumption, and has incomparable superiority compared with the prior art.

Description

technical field [0001] The invention relates to a method for liquid-phase selective hydrogenation of carbon three fractions. Background technique [0002] Steam cracking of petroleum hydrocarbons is the most important method for preparing polyolefin monomers such as propylene. The alkynes and dienes produced in the propylene production process are harmful impurities that affect the propylene polymerization reaction. They will inhibit the activity of the propylene polymerization catalyst, increase the consumption of the catalyst, and reduce the properties of the propylene polymer product, so they must be removed. In industry, catalytic selective hydrogenation and solvent absorption are usually used to remove alkynes and dienes in cracked gas. The process of catalytic selective hydrogenation is simple, the selectivity of propylene is high, the rich product is less, and there is no environmental pollution. It is the preferred method of green chemical process and its applicatio...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C11/06C07C7/163C07C7/167
CPCC07C7/005C07C7/163C07C7/167C07C11/06
Inventor 易水生房艳乐毅毛祖旺彭晖
Owner CHINA PETROLEUM & CHEM CORP
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