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Method for liquid phase selective hydrogenation of C3 hydrocarbons

A selective hydrogenation and three-liquid-phase technology, which is applied in the field of liquid-phase selective hydrogenation of propyne and/or propadiene to generate propylene, can solve the problems of increased catalyst consumption, reduced catalyst activity, and poor properties of propylene polymers. Achieve the effects of being beneficial to the propylene rectification process, convenient operation, and small investment in equipment

Active Publication Date: 2011-05-04
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
  • Method for liquid phase selective hydrogenation of C3 hydrocarbons

Examples

Experimental program
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Embodiment 1

[0052] according to figure 1 The flow process of the shown carbon three liquid phase selective hydrogenation of the present invention is that the content of propyne and propadiene (MAPD) ​​is 6.7mol%, and the fresh carbon three cut f of 65.7 ton / h is mixed with hydrogen b, and the hydrogen The 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 combines with the carbon three-phase liquid phase selective hydrogenation catalyst BC-L- 83 (provided by Sinopec Beijing Research Institute of Chemical Industry), the reactor pressure was 2.60MPa, the reactor inlet temperature was 35°C, and the reactor outlet temperature was 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 bo...

Embodiment 2

[0058] according to image 3 The carbon three flow process of the present invention, with propyne and propadiene (MAPD) ​​content is 6.7mol%, the fresh carbon three fraction f of flow rate is 65.7ton / h is mixed with hydrogen b, and hydrogen flow rate is 380kg / h, the obtained mixture Enter the reactor from the top of the selective hydrogenation reactor, pass through the selective hydrogenation catalyst bed in the reactor from top to bottom, and contact with the carbon three-phase liquid phase selective hydrogenation catalyst BC-L-83, the reactor pressure is 2.60MPa, The reactor inlet temperature was 35°C and the reactor outlet temperature was 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 separa...

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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 reactiontower (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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Patent Type & Authority Patents(China)
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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