A fixed-bed dehydrogenation process for low-carbon alkanes

A low-carbon alkanes, fixed-bed technology, applied in the fields of butane dehydrogenation to butene and propane dehydrogenation to propylene, to achieve the effect of reducing the amount of B acid, low equipment investment, and improved anti-carbon deposition performance

Active Publication Date: 2020-04-10
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0006] CN1213662A discloses a kind of dehydrogenation process technology of isobutane, dehydrogenation reaction is to carry out in fluidized bed reactor, used catalyst is chromium series microsphere catalyst, the catalyst of this process can be regenerated continuously, and production can carry out continuously, but The manufacture, use and recycling of chromium-based catalysts for fluidized beds have strict environmental protection requirements

Method used

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  • A fixed-bed dehydrogenation process for low-carbon alkanes
  • A fixed-bed dehydrogenation process for low-carbon alkanes

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0040] 223g (NH 4 ) 2 Cr 2 o 7 Dissolve in 800ml ethylene glycol, impregnate equal volume to 1000g porous γ-Al 2 o 3 in powder. The powder was placed in an oven at 120°C for 4 hours, washed with deionized water, filtered, and dried at 80°C for 2 hours. 37g KNO 3 Dissolved in 800ml of deionized water, impregnated into the above treated powder with equal volume, dried at 80°C for 4 hours, calcined at 680°C for 5 hours, and the catalyst obtained by forming and sieving was designated as Catalyst A.

[0041] Butane dehydrogenation:

[0042] Reaction process conditions, reaction temperature 590°C, pressure 0.11MPa, butane mass space velocity 1.0h -1 , the filling amount of the inert carrier is 100wt.% of the filling amount of catalyst A, the reaction time is 0.7h; the regeneration gas is air, the regeneration temperature is 660°C, the regeneration pressure is 0.10MPa, and the volume space velocity is 1000h -1 , regeneration time is 0.6h, nitrogen stripping space velocity is...

Embodiment 2

[0052] 177g CrO 3 , 248g (NH 4 ) 2 C 2 o 4 Dissolve in 800ml deionized water, impregnate equal volume into 1000g porous γ-Al 2 o 3 in powder. The powder was placed in an oven at 60°C for 6 hours, washed with deionized water, filtered, and dried at 100°C for 2 hours. 78gCu(NO 3 ) 2 ·3H 2 O, 112g Fe(NO 3 ) 3 9H 2 O was dissolved in 700ml of deionized water, impregnated into the above-mentioned treated powder with an equal volume, dried at 120°C for 3 hours, calcined at 700°C for 6 hours, and the catalyst obtained by forming and sieving was designated as Catalyst C.

[0053] Butane dehydrogenation:

[0054] Reaction process conditions, reaction temperature 585°C, pressure 0.11MPa, mass space velocity of butane 2.5h -1 , the loading amount of the inert carrier is 200wt.% of the loading amount of catalyst C, the reaction time is 0.5h; the regeneration gas is air, the regeneration temperature is 670°C, the regeneration pressure is 0.10MPa, and the volume space velocity...

Embodiment 3

[0064] 130g K 2 Cr 2 o 7 Dissolve in 800ml glycerol, impregnate equal volume into 1000g porous γ-Al 2 o 3 in powder. The powder was placed in an oven at 140°C for 1 hour, washed with deionized water, filtered, and dried at 80°C for 4 hours. 33g NaNO 3 , 82g Ni(NO 3 ) 2 ·6H 2 O was dissolved in 800ml of deionized water, impregnated into the above-mentioned treated powder with an equal volume, dried at 60°C for 6 hours, calcined at 720°C for 4 hours, and the catalyst obtained by forming and sieving was designated as Catalyst E.

[0065] Butane dehydrogenation:

[0066] Reaction process conditions, reaction temperature 610°C, pressure 0.2MPa, butane mass space velocity 0.5h -1 , the filling amount of the inert carrier is 50wt.% of the filling amount of the catalyst D, and the reaction time is 0.2h; the regeneration gas is air, the regeneration temperature is 650°C, the regeneration pressure is 0.10MPa, and the volume space velocity is 3000h -1 , regeneration time is 0....

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Abstract

The invention discloses a low-carbon alkane dehydrogenation process method. According to the low-carbon alkane dehydrogenation process method, a fixed bed process is used, and a chromium-based low-carbon alkane dehydrogenation catalyst is loaded; and the catalyst preparation method comprises: dissolving a high-valent chromium precursor in a reducing agent solution, impregnating into an alumina-based carrier, washing, filtering, and drying to prepare the catalyst. According to the present invention, by combining the catalyst and the fixed bed process, the whole dehydrogenation process has advantages of simple process, low investment on equipment, low catalyst cost, strong stability, high low-carbon alkane conversation rate, and good selectivity.

Description

technical field [0001] The invention relates to a process for dehydrogenating low-carbon alkanes, in particular to a process for producing butene by dehydrogenating butane and producing propylene by dehydrogenating propane. Background technique [0002] In recent years, with the rapid development of the global petrochemical industry, the demand for low-carbon olefins is also increasing. The catalytic dehydrogenation technology of light alkanes is an effective way to increase the production of C3-C4 olefins. [0003] The catalytic dehydrogenation reaction of light alkanes is limited by thermodynamic equilibrium, and must be carried out under harsh conditions of high temperature and low pressure. Excessively high temperature will intensify the cracking reaction and deep dehydrogenation of alkane, and reduce the selectivity; at the same time, it will accelerate the surface carbon of the catalyst and make the catalyst deactivate rapidly. Therefore, the catalyst needs to be reg...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): B01J23/26B01J23/86C07C5/333C07C11/06C07C11/08
CPCB01J23/002B01J23/26B01J23/862B01J23/864B01J23/866B01J23/868B01J2523/00C07C5/3332C07C2523/26C07C2523/86B01J2523/13B01J2523/31B01J2523/67B01J2523/17B01J2523/842B01J2523/12B01J2523/847B01J2523/3706B01J2523/23B01J2523/24B01J2523/845C07C11/06C07C11/08Y02P20/52
Inventor 李长明周金波李博王艳飞李秋颖程中克苟文甲董炳利唐迎春马艳捷
Owner PETROCHINA CO LTD
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