In-situ regeneration method of butylene oxy-dehydrogenation catalyst

A technology of oxidative dehydrogenation and in-situ regeneration, which is applied in the direction of catalyst regeneration/reactivation, metal/metal oxide/metal hydroxide catalyst, physical/chemical process catalyst, etc., and can solve the problems affecting the extension of catalyst life and reaction conversion efficiency, reaction yield, poor in-situ regeneration effect of butene oxidative dehydrogenation catalyst, and long shutdown time of the device, so as to achieve the effects of preventing carbon formation, recovery of activity, and shortened shutdown time

Inactive Publication Date: 2013-05-01
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
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Problems solved by technology

[0015] The technical problem mainly solved by the present invention is that the in-situ regeneration effect of the butene oxidative dehydrogenation catalyst in the prior art is not good, thereby affecting the prolongation of the catalyst life, the reaction conversion rate, the reaction yield, and the shutdown time of the device caused by catalyst replacement Long, the problem that affects the output of the device

Method used

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  • In-situ regeneration method of butylene oxy-dehydrogenation catalyst

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Embodiment 1

[0042] A 100,000 tons / year butene oxidative dehydrogenation to butadiene plant adopts figure 1 The process technology adopts an iron-based catalyst, its main composition includes iron, zinc, and magnesium components, and the molar ratio of each component is: Fe:Zn:Mg=10:2:5, prepared by coprecipitation method, the main crystal Phase is ZnFe 2 o 4 Spinel, the reactor is two-stage, and the two-stage reactor is an adiabatic radial fixed-bed reactor. The total amount of raw material butene is 19670kg / h, the total amount of air is 36000 kg / h, and the total amount of water vapor is 66000 kg / h. The butene raw material is divided into two parts. The flow rate of butene in the first stage is 9400 kg / h. After mixing with air and water vapor according to the ratio of butene: oxygen: water (mol) of 1:0.52:15, the temperature is 320°C and the pressure is Under the condition of 0.12MPaG, it enters the first-stage oxidative dehydrogenation reactor. The outlet gas temperature of the first-s...

Embodiment 2

[0046] A 100,000 tons / year butene oxidative dehydrogenation to butadiene plant adopts figure 1 The process technology adopts an iron-based catalyst, its main composition includes iron, zinc, and magnesium components, and the molar ratio of each component is: Fe: Zn: Mg=10:2:6, prepared by coprecipitation method, the main crystal Phase is ZnFe 2 o 4 Spinel, the reactor is three-stage, all three-stage reactors are adiabatic radial fixed-bed reactors, the total amount of raw material butene is 18920kg / h, the total amount of air is 36000 kg / h, the total amount of water vapor is 47500 kg / h, The butene raw material is divided into three parts. The flow rate of butene in the first stage is 9200 kg / h. After mixing with air and water vapor according to the ratio of butene: oxygen: water (mol) of 1:0.5:15, the temperature is 320 °C and the pressure is Under the condition of 0.13MPaG, it enters the first-stage oxidative dehydrogenation reactor. The outlet gas temperature of the first-s...

Embodiment 3

[0050] A 100,000 tons / year butene oxidative dehydrogenation to butadiene plant adopts figure 1 The process technology uses an iron-based catalyst whose main composition is Fe 2 o 3 · MgO · ZnO · P 2 o 5 ·ZnxOy, the reactor is two-stage, and the two-stage reactors are adiabatic radial fixed-bed reactors. The total amount of raw material butene is 19,670 kg / h, the total amount of air is 36,000 kg / h, and the total amount of water vapor is 30,200 kg / h. The olefin raw material is divided into two parts. The flow rate of butene in the first stage is 9400 kg / h. After mixing with air and water vapor according to the ratio of butene: oxygen: water (mol) of 1:0.52:10, the temperature is 330 °C and the pressure is 0.12. Under the condition of MPaG, it enters the first-stage oxidative dehydrogenation reactor. The outlet gas temperature of the first-stage reactor is 495°C. The flow rate of butene is 10270 kg / h, the ratio of butene:oxygen:water (mol) at the inlet of the secondary reacto...

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Abstract

The invention relates to an in-situ regeneration method of a butylene oxy-dehydrogenation catalyst, which mainly solves the problems that the in-situ regeneration effect of the butylene oxy-dehydrogenation catalyst is poor, so that the life of the catalyst is shortened, the conversion rate and yield of reaction are reduced, and the change of the catalyst results in long stopping time of a device and influences the output of the device in the prior art. The method comprises the following steps of: a) stopping feeding of oxygen-containing gas and then a butylene raw material, purging the catalyst with 300-500 DEG C superheated water vapor for 0.2-56h, b) gradually reducing the amount of the water vapor till the airspeed of the water vapor is 500-2000h<-1>, filling in air till the molar ratio of the air to the water vapor is 0.05-0.2, controlling the regeneration temperature at 360-450 DEG C, conducting regeneration of the oxy-dehydrogenation catalyst, and c) reducing the amount of the vapor, allowing the temperature rise of a bed to be reduced gradually till the temperature at an inlet and an outlet of the catalyst bed keeps constant, and accomplishing the technical scheme of catalyst regeneration. The method solves the problems better, and can be used for industrial production of preparing butadiene through butylene oxy-dehydrogenation.

Description

technical field [0001] The invention relates to an in-situ regeneration method of a butene oxidation dehydrogenation catalyst. Background technique [0002] Butadiene is an important monomer of synthetic rubber and synthetic resin, mainly used in the synthesis of butadiene rubber, styrene-butadiene rubber, nitrile rubber and ABS resin. Butadiene is also a variety of coatings and organic chemical raw materials. [0003] At present, butadiene is mainly produced in two ways: separation of C4 fractions and synthesis (including butane dehydrogenation, butene dehydrogenation, butene oxidative dehydrogenation, etc.). At present, except the United States, almost all butadiene in the world comes directly from the by-product C4 fraction (also written as C4 fraction) when hydrocarbons are cracked to produce ethylene. About half of the sources of butadiene in the United States come from the dehydrogenation of butane and butene, and half come directly from cracking C4 fractions. [00...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J38/06B01J38/12B01J23/94B01J23/80B01J27/28B01J27/185C07C11/167C07C5/48
CPCY02P20/584
Inventor 刘文杰吴文海张洪宇
Owner CHINA PETROLEUM & CHEM CORP
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