C3 fraction selective hydrogenation method

A selective hydrogenation and fractionation technology, which is applied to hydrocarbons, chemical instruments and methods, purification/separation of hydrocarbons, etc., can solve problems such as increasing the difficulty of operation

Active Publication Date: 2014-10-15
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

This method also increases

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0051] A commercially available bimodal pore distribution cylindrical alumina carrier with a diameter of 4 mm and a length of 4 mm was used. After calcination at 1100°C for 4 hours, the bimodal peaks of pore diameters are at 40nm and 100nm respectively, the pore volume is 0.6ml / g, and the specific surface area is 60m 2 / g.

[0052] Its C3 fraction comes from sequential hydrogenation processes such as figure 1 As shown, but the reaction bed of the adiabatic bed reactor is divided into two sections, and the raw material composition is shown in Table 1.

[0053] Table 1 hydrogenation raw material composition

[0054] Hydrogenation feedstock

C 3 h 4 (MA)

C 3 h 4 (PD)

C 3 h 6

C 3 h 8

Content (v / v%)

4.8

3.2

82.0

10.0

[0055] Reaction conditions:

[0056] Two-stage adiabatic bed reactor hydrogenation process, liquid phase raw material volume space velocity: 5h -1 , Operating pressure: 2.5MPa, reactor catalys...

Embodiment 2

[0058] A commercially available bimodal pore distribution spherical alumina carrier with a diameter of 4 mm was used. After calcination at 1050°C for 4 hours, the bimodal peaks of pore diameters are at 20nm and 150nm respectively, the pore volume is 0.4ml / g, and the specific surface area is 70m 2 / g.

[0059] use figure 1 The technological process shown, its C3 fraction raw material composition is as shown in Table 2.

[0060] Table 2 hydrogenation raw material composition

[0061] Hydrogenation feedstock

[0062] Single-stage reactor hydrogenation process, liquid phase raw material volume space velocity: 50h -1 , Operating pressure: 3.5MPa, reactor catalyst loading: 300ml, hydrogen / (MA+PD) (mol)=5:1, reactor inlet temperature 25°C. The reaction results after 1000 hours of assessment are shown in Table 5.

Embodiment 3

[0064] A commercially available bimodal pore distribution four-leaf clover-shaped alumina carrier was used, with a diameter of 5.5 mm and a length of 4 mm. After calcination at 1000°C for 4 hours, the bimodal peaks of pore diameters are 30nm and 200nm respectively, the pore volume is 0.5ml / g, and the specific surface area is 80m 2 / g.

[0065] use figure 2 The technological process shown, its C3 fraction raw material composition is as shown in Table 5.

[0066] Table 3 hydrogenation raw material composition

[0067] Hydrogenation feedstock

C 3 h 4 (MA)

C 3 h 4 (PD)

C 3 h 6

C 3 h 8

Content (mol%)

0.1

0.1

85.0

14.80

[0068] Reaction process conditions: single-stage adiabatic bed reactor process, material space velocity: 100h -1 , Operating pressure: 3.0MPa, catalyst loading: 200ml. Hydrogen / (MA+PD)(mol)=1:1. The reaction results after 600 hours of assessment are shown in Table 6.

[0069] Embodiment ...

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Abstract

The invention relates to a C3 fraction selective hydrogenation method. The C3 fraction selective hydrogenation method comprises the following steps of feeding a C3 fraction into an adiabatic bed reactor, and carrying out selective hydrogenation to remove allylene and allene. The C3 fraction selective hydrogenation method is characterized in that selective hydrogenation catalyst carriers comprise alumina or mainly comprise alumina, have double-humped hole distributed structures and contain double active components of Pd and Ni. In catalyst preparation, a coking-resistant component Ni in the form of microemulsion enters into large holes of the carriers so that the coking-resistant component Ni is mainly distributed in the large holes of the carriers and thus a catalyst surface coking degree is greatly reduced, the compound subjected to hydrogenation saturation is gradually diffused into catalyst channels, channel blocking is avoided, a catalyst service life is greatly prolonged, a green oil yield and catalyst coking are obviously reduced and device operation economic benefits are improved.

Description

technical field [0001] The invention relates to a method for selective hydrogenation, in particular to a method for selective hydrogenation of carbon three fractions to remove acetylene. Background technique [0002] The acquisition of high-purity propylene is the prerequisite for the production of polypropylene, and the key to the production of high-purity propylene is to remove propyne (MA) and propadiene (PD) in the C3 fraction, generally by selective hydrogenation. [0003] The current hydrogenation process mainly adopts liquid-phase hydrogenation. Since propyne and propadiene (MA+PD) in the carbon three components have a strong tendency to polymerize, it is easy to form coke on the surface of the catalyst. As a result, the activity of the catalyst is reduced, the quality of the hydrogenation product is unqualified, and the operating life of the catalyst is shortened. [0004] In the hydrogenation process of C3 fraction without prehydrogenation, that is, in the sequenti...

Claims

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Application Information

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IPC IPC(8): C07C11/06C07C7/167C07C7/163B01J23/89
CPCY02P20/52
Inventor 谭都平梁琨张峰车春霞颉伟韩伟梁玉龙高源钱颖李赫常晓昕胡晓丽林宏刘晓兰
Owner PETROCHINA CO LTD
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