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Method for liquid phase selective hydrogenation of C3 hydrocarbons

A technology of selective hydrogenation and three liquid phases, applied in the field of liquid phase selective hydrogenation of propyne and/or propadiene to generate propylene, can solve the problems of increasing catalyst consumption, worsening properties of propylene polymers, reducing catalyst activity and the like, It is beneficial to the propylene rectification process, the equipment investment is small, and the operation is convenient.

Active Publication Date: 2008-03-12
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The alkynes and dienes produced in this process are harmful impurities that affect the propylene polymerization reaction. They will reduce the activity of the propylene polymerization catalyst, increase the consumption of the catalyst, and also make the properties of the generated propylene polymer worse, so they must be removed remove

Method used

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  • Method for liquid phase selective hydrogenation of C3 hydrocarbons
  • Method for liquid phase selective hydrogenation of C3 hydrocarbons

Examples

Experimental program
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Effect test

Embodiment 1

[0052] According to the flow process of the carbon three liquid phase selective hydrogenation of the present invention shown in Fig. 1, propyne and propadiene (MAPD) ​​content is 6.7mol%, and flow rate is the fresh carbon three fraction f of 65.7ton / h and hydrogen b Mixing, the hydrogen flow rate is 380kg / h, the obtained mixture enters the reactor from the top of the selective hydrogenation reactor, passes through the selective hydrogenation catalyst bed in the reactor from top to bottom, and the carbon three-phase liquid phase selective hydrogenation catalyst BC -L-83 (provided by Sinopec Beijing Research Institute of Chemical Industry), the reactor pressure is 2.60MPa, the reactor inlet temperature is 35°C, and the reactor outlet temperature is 60°C. After the selective hydrogenation reaction, the output c at the bottom of the reactor mainly contains propylene, propane and MAPD with a content of less than 200ppm. The material c discharged from the bottom of the reactor direc...

Embodiment 2

[0058] According to Fig. 3 C3 flow process of the present invention, propyne and propadiene (MAPD) ​​content is 6.7mol%, flow is the fresh C3 fraction f of 65.7ton / h and hydrogen b is mixed, and hydrogen flow is 380kg / h, so The obtained mixture enters the reactor from the top of the selective hydrogenation reactor, passes through the selective hydrogenation catalyst bed in the reactor from top to bottom, and contacts with the carbon three liquid phase selective hydrogenation catalyst BC-L-83, and the reactor pressure is 2.60MPa, the reactor inlet temperature is 35°C, and the reactor outlet temperature is 60°C. After the selective hydrogenation reaction, the output c from the bottom of the reactor contains propylene, propane and MAPD with a content of less than 200ppm. The material c at the bottom of the reactor tower directly enters a gas-liquid separation tank for gas-liquid two-phase separation, and the pressure of the gas-liquid separation tank is 2.56 MPa. The gas phase s...

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Abstract

The present invention discloses a selective hydrogenation method for a liquid phase of a carbon fractionation, which relates to a selective hydrogenation method to prepare propylene by propine and or propadiene included in the carbon fractionation from the tower top of depropanization in the manufacturing process for propylene. The method is that: the carbon fractionation is firstly mixed with hydrogen, and then the mixture enters a reaction device from the top of the reaction device; after being made with the selective hydrogenation reaction, the heat material from the bottom of the reaction tower (the mixture between the liquid and the gas) does not take the heat exchange process, and directly enters an air-liquid separated pot to be separated. The air-phase part enters a condensator arranged on or on the upper part of the separated pot; the liquid after being condensed is taken as a product to be inducted; the non-condensed air-phase part discharges or is sent to a fuel air-tube net or the entrance of the second section or the third section or the fourth section of a compressor; the pressure inside of the reaction device is adjusted by controlling the temperature in the consensator or by controlling the air-phase flow for the discharging.

Description

technical field [0001] The present invention relates to the method for the liquid-phase selective hydrogenation of propyne and / or propadiene to generate propylene, especially the liquid-phase selective hydrogenation of propyne and / or propadiene contained in the carbon three cuts in the production process of propylene Method for producing propylene. 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 this process are harmful impurities that affect the propylene polymerization reaction. They will reduce the activity of the propylene polymerization reaction catalyst, increase the consumption of the catalyst, and also make the properties of the generated propylene polymer worse, so they must be removed remove. In industry, catalytic selective hydrogenation and solvent absorption are usually used to remove alkynes and dienes in cracked gas. Du...

Claims

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Application Information

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IPC IPC(8): C07C11/06C07C5/02C07C5/09
Inventor 戴伟张立岩郭彦来彭晖卫国宾汪晓菁卢红亮王晓静
Owner CHINA PETROLEUM & CHEM CORP
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