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Catalyst loading method for isothermal reactor

A technology for isothermal reactors and catalysts, applied in chemical instruments and methods, organic chemistry, chemical recovery, etc., can solve the problems of low butadiene selectivity, catalyst carbon deposition regeneration cycle, etc., to improve conversion rate and selectivity, The effect of saving product yield and improving production capacity

Active Publication Date: 2016-08-24
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
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Problems solved by technology

[0014] The main technical problem to be solved by the present invention is that the local temperature of the tubes in the reactor is too high, the selectivity of butadiene is low, the carbon deposition of the catalyst and the regeneration cycle exist in the butene oxidative dehydrogenation tubular isothermal reactor technology in the prior art. The short question is to provide a new catalyst loading method for butene oxidative dehydrogenation isothermal reactor, which has the advantages of easy control of catalyst temperature in isothermal reactor tubes, no carbon deposition, long regeneration period and butadiene selectivity high advantage

Method used

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  • Catalyst loading method for isothermal reactor
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  • Catalyst loading method for isothermal reactor

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Embodiment 1

[0030] A 200,000 tons / year butene oxidative dehydrogenation to butadiene plant adopts figure 1 The reactor is an isothermal tubular fixed bed reactor, the size of the reactor is Φ4500×6000mm, the tubes are Φ50×6000mm, the number of tubes is 4000, and the heat exchange area is 3900m 2 , the catalyst is two kinds of A agent and B agent, A agent is an iron-based composite oxide catalyst, and its general formula is Fe according to its chemical composition. 2 o 3 · MgO · ZnO · P 2 o 5 · CuO, Fe 2 o 3 66% of the catalyst weight, MgO is 20% of the catalyst weight, ZnO is 10% of the catalyst weight, P 2 o 5 CuO is 2% of the weight of the catalyst, and CuO is 2% of the weight of the catalyst, prepared by coprecipitation; agent B is an iron oxide catalyst, the weight content of iron, zinc, and magnesium oxide is 40%, and the weight content of inert alumina is 60% %, the molar ratio of iron, zinc and magnesium is: Fe:Zn:Mg=10:3:5, and the main crystal phase is ZnFe 2 o 4 Spinel,...

Embodiment 2

[0035] A 200,000 tons / year butene oxidative dehydrogenation to butadiene plant adopts figure 1 The reactor is an isothermal tubular fixed bed reactor, the size of the reactor is Φ4500×6000mm, the tubes are Φ50×6000mm, the number of tubes is 4000, and the heat exchange area is 3900m 2 , the catalyst is two kinds of A agent and B agent, A agent is an iron-based composite oxide catalyst, and its general formula is Fe according to its chemical composition. 2 o 3 · MgO · ZnO · P 2 o 5 · MnO 2 , Fe 2 o 3 66% of the catalyst weight, MgO is 20% of the catalyst weight, ZnO is 10% of the catalyst weight, P 2 o 5 2% of catalyst weight, MnO 2 It is 2% of the weight of the catalyst, prepared by co-precipitation method; agent B is an iron-based oxide catalyst, the weight content of iron, zinc, and magnesium oxide is 40%, the weight content of inert alumina is 60%, and the molar content of iron, zinc, and magnesium The ratio is: Fe:Zn:Mg=10:3:5, the main crystal phase is ZnFe 2 o ...

Embodiment 3

[0040] A 200,000 tons / year butene oxidative dehydrogenation to butadiene plant adopts figure 1 The reactor is an isothermal tubular fixed-bed reactor, the size of the reactor is Φ4000×6000mm, the tubes are Φ50×6000mm, the number of tubes is 3400, and the heat exchange area is 3300m 2 , the catalyst is two kinds of A agent and B agent, A agent is an iron-based composite oxide catalyst, and its general formula is Fe according to its chemical composition. 2 o 3 · MgO · ZnO · P 2 o 5 · NiO, Fe 2 o 3 62% of the catalyst weight, MgO is 21% of the catalyst weight, ZnO is 12% of the catalyst weight, P 2 o 5 It is 2% of the weight of the catalyst, and NiO is 3% of the weight of the catalyst. It is prepared by co-precipitation method; agent B is inert alumina ceramic balls, and the tubes are divided into 4 filling areas from the inlet of the reaction gas to the outlet, and the filling areas are segmented The length and the content of A and B agents are shown in Table 3. The tota...

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Abstract

The invention relates to a filling method for a butane oxydehydrogenation isothermal reactor catalyst. The filling method mainly solves the problems that in the butane oxydehydrogenationn array pipe type isothermal reactor technology in the prior art, the local temperature of an array pipe in a reactor is too high, the butadiene selectivity is low, the catalyst carbon deposit occurs, and the regeneration period is short. The filling method adopts the technical scheme that the adopted reactor is the array pipe type isothermal reactor, and a mixture of catalysts A and catalysts B is filled in the array pipe, wherein the catalysts A are high-activity catalysts, and the catalysts B are low-activity catalysts or inert materials. During the catalyst filling, the array pipe is divided into N filling regions from a raw material inlet and a raw material outlet, wherein N is greater than or equal to 2, and is an integer representing the number of the filling regions. The catalysts A and the catalysts B with different mixing proportions are filled in different filling regions. The problems are perfectly solved, and the filling method can be used for the industrial production for preparing butadiene from butane through oxydehydrogenation.

Description

technical field [0001] The invention relates to a catalyst loading method for a butene oxidative dehydrogenation isothermal reactor. 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 hydrocarbon cracking is used 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 fractio...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): B01J8/06C07C11/16C07C5/48
CPCY02P20/584
Inventor 刘文杰吴文海
Owner CHINA PETROLEUM & CHEM CORP
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