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Method for selective hydrogenation of C2 fraction

A technology for selective hydrogenation and fractionation, which is used in chemical instruments and methods, hydrogenation to hydrocarbons, and bulk chemical production. big effect

Active Publication Date: 2013-07-31
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0014] But the contriver finds, this technology is effective to heavier green oil component, but to the lighter component that generates in the reaction, especially carbon four distillate then effect is relatively poor, and these lighter components enter second-stage processing After the hydrogen reactor, it will still have a serious impact on the performance of the catalyst, and even reduce the performance of the catalyst by more than 80%, resulting in a shortened catalyst operation cycle and a decrease in the purity of ethylene products

Method used

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  • Method for selective hydrogenation of C2 fraction
  • Method for selective hydrogenation of C2 fraction
  • Method for selective hydrogenation of C2 fraction

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0033] Preparation of polymerization catalyst:

[0034] Weigh γ-Al 2 O 3 500g, add 158.75g of Fe 2 (SO 4 ) 3 ·6H 2 O, 157g NiSO 4 ·6H 2 O, added to deionized water together, immersed in constant temperature for 3 hours, dried at 100°C for 4 hours, and then placed the catalyst in a muffle furnace at 300°C and calcined for 4 hours to obtain a polymerization catalyst.

[0035] Adopt attached figure 1 The process flow shown. Three-stage carbon two hydrogenation reactor process, each stage hydrogenation reactor catalyst loading capacity is 300ml, reactor space velocity 4500 / h, the first stage hydrogenation reactor inlet acetylene 2.1 (V / V%), ethylene 85.2 (V / V%), ethane 12.7 (V / V%), the inlet temperature of the first stage hydrogenation reactor is 45°C, the reactor outlet temperature is 95°C, the catalyst is G-58C, and the reaction pressure is 2.0MPa. The polymerization reactor is located between the first-stage hydrogenation reactor and the subsequent heat exchanger. The reactor is...

Embodiment 2

[0041] Preparation of polymerization catalyst:

[0042] Weigh γ-Al 2 O 3 500g, add 68g of Fe 2 (SO 4 ) 3 ·6H 2 O, 27.2g NiSO 4 ·6H 2 O, added to deionized water together, immersed in constant temperature for 2 hours, dried at 80°C for 8 hours, and then placed the catalyst in a muffle furnace at 500°C and calcined for 5 hours to obtain a polymerization catalyst.

[0043] Adopt attached figure 1 The process flow shown. Adopting three-stage carbon two hydrogenation reactor process, each stage hydrogenation reactor catalyst loading volume is 500ml, reactor space velocity is 6500 / h, the first stage hydrogenation reactor inlet acetylene 1.6 (V / V%), ethylene 81.6 ( V / V%), ethane 16.8 (V / V%). The inlet temperature of the first stage hydrogenation reactor is 45°C, the reactor outlet is 75°C, the catalyst is G-58C, and the reaction pressure is 2.5MPa. The polymerization reactor is located between the first-stage hydrogenation reactor and the first-stage post-heat exchanger. The reactor i...

Embodiment 3

[0049] Preparation of polymerization catalyst:

[0050] Weigh 384.7g γ-Al 2 O 3 , 340.0g of Fe 2 (SO 4 ) 3 ·6H 2 O, 163.75g NiSO 4 ·6H 2 O, added to deionized water together, immersed in constant temperature for 4h, dried at 150℃ for 2h, and then placed the catalyst in a muffle furnace at 500℃ for 3h. Then 42.49 g of silicic acid was added, stirred for 30 minutes, and calcined at 500° C. for 4 hours to obtain a polymerization catalyst.

[0051] Adopt attached figure 1 The process flow shown. Three-stage carbon two hydrogenation reactor process, each stage hydrogenation reactor catalyst loading capacity is 500ml, reactor space velocity 5000 / h, the first stage hydrogenation reactor inlet acetylene 2.2% (V / V), ethylene 80.6 (V / V%), ethane 17.2 (V / V%). The inlet temperature of the first stage hydrogenation reactor is 40℃, and the catalyst is LY-C 2 -02, the reaction pressure is 2.0MPa. The polymerization reactor is located between the first-stage hydrogenation reactor and the heat...

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Abstract

The invention discloses a method for selective hydrogenation of C2 fraction. The C2 fraction, which comes from a dethanizing column, in an ethylene device is aerated with hydrogen and then enters a fixed bed catalytic hydrogenation reactor for selective hydrogenation so as to remove acetylene from the C2 fraction, wherein the fixed bed catalytic hydrogenation reactor is a plurality of sections offixed bed catalytic hydrogenation reactors. The method is characterized in that: among the plurality of sections of fixed bed catalytic hydrogenation reactors, the C2 fraction undergoes the polymerization reaction besides the selective hydrogenation reaction; a polymerization catalyst is used; and the polymerization catalyst is a Fe2(SO4)3-NiSO4 / Al2O3 catalyst. By the method, the amount of C4 olefin is greatly reduced after a polymerization reaction is added, and the contaminated degree of second-stage and three-stage hydrogenation catalysts is greatly reduced.

Description

Technical field [0001] The invention relates to a selective hydrogenation method, in particular to a method for selective hydrogenation of carbon two fractions to remove acetylene. Background technique [0002] Polymer-grade ethylene production is the leader of the petrochemical industry. Polymer-grade ethylene and propylene are the most basic raw materials for downstream polymerization devices. In addition to ensuring that the acetylene content at the outlet of the hydrogenation reactor meets the standard, the selectivity of the catalyst is excellent, which can minimize ethylene. The formation of ethane is of great significance for increasing the ethylene yield of the entire process and improving the economic benefits of the device. [0003] The cracked carbon two fraction contains 0.5% to 2.5% (V / V%) of acetylene. When producing polyethylene, a small amount of acetylene in ethylene will reduce the activity of the polymerization catalyst and make the physical properties of the pol...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C11/04C07C5/09B01J27/053B01J27/185
CPCY02P20/52
Inventor 谭都平车春霞梁琨景喜林梁玉龙林宏李耀高源颉伟常晓昕梁顺琴黄德华
Owner PETROCHINA CO LTD