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Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO)

A fluidized bed reactor, methanol-to-olefin technology, applied in hydrocarbon cracking to hydrocarbon production, chemical instruments and methods, organic chemistry, etc., can solve the problem of back-mixing of catalyst and oil and gas, reducing gas-solid contact efficiency, low single-pass conversion rate, etc. It can reduce the back-mixing of gas, improve the contact reaction efficiency, and improve the gas-solid contact efficiency.

Inactive Publication Date: 2015-03-25
CHINA UNIV OF PETROLEUM (EAST CHINA)
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] However, if the riser reactor in the catalytic cracking process is used, the catalyst in it is in a state of dilute phase transport, and light olefins or methanol dispersed in molecular form cannot fully contact with the catalyst, so the conversion rate per pass is not high; if bubbling is used bed or turbulent bed, the back-mixing of catalyst and oil and gas is relatively serious, resulting in the secondary reaction of the target product small molecular olefins into low value-added products, and it is easy to form large bubbles or grooves in the dense phase section of these two types of fluidized beds flow phenomenon, thereby reducing the efficiency of gas-solid contact

Method used

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  • Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO)
  • Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO)
  • Fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO)

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Effect test

Embodiment 1

[0047] like Figure 1-3 As shown, a high gas-solid contact efficiency dense-phase fluidized bed reactor for light olefin cracking and methanol to olefin of the present invention includes a reactor, a settler 12, a catalyst standby inclined tube 9, and a catalyst regenerator 11 , a pre-riser 3 and a catalyst regeneration inclined pipe 7; the reactor includes a dense-phase fluidized bed reactor 1 and a dilute-phase conveying reactor 2, and the dense-phase fluidized-bed reactor 1 and the dilute-phase conveying reactor 2 are in On the same axis, the pre-lift pipe 3 and the dilute-phase transport reactor 2 are respectively located at the upper and lower parts of the dense-phase fluidized-bed reactor 1; the diameter of the pre-lift pipe 3 is smaller than the diameter of the dense-phase fluidized-bed reactor 1, and the pre-lift The upper part of the pipe 3 extends into the dense phase fluidized bed reactor 1 . From the upper port of the pre-riser 3 to the bottom of the dense-phase f...

Embodiment 2

[0055] The catalysts used in the reaction example of methanol to olefins are industrial LTB-8 catalysts, and the active component is hierarchically porous HZSM-11 molecular sieve (ZL201210003750.5). After aging for 4 hours under steam conditions, it is ready for use.

[0056] The dense-phase fluidized bed reactor shown in appendix 2 is installed in such as appendix figure 1 In the circulating fluidized bed reaction regeneration device shown, the LTB-8 catalyst of 20kg aging is loaded into as attached figure 1 The circulating fluidized bed reaction regeneration device shown. A 3-layer grid is installed between the feed distributor and the outlet of the pre-lift pipe, and the distance between the grids is 0.4m. The feed rate of pure methanol is 4kg / h, preheated to 200°C, and enters the dense-phase fluidized bed reactor through the feed distributor, and the reaction temperature is controlled at 500°C; the average line of the gas in the dense-phase fluidized bed reactor The vel...

Embodiment 3

[0059] Other conditions are identical with embodiment 2, and the pure methanol feed rate is reduced to 1.5kg / h, and the gas average linear velocity in the dense phase fluidized bed reactor is 0.3m / s, and the average residence time is about 2.0s; The average linear velocity in the dilute phase region is 3.0m / s, and the average residence time is about 1.8s. The reaction results are shown in attached table 1, the conversion rate is similar to that of Example 1, but due to the long residence time of oil and gas in the reactor, the content of ethylene and propylene in dry gas and liquefied gas has decreased.

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Abstract

The invention discloses a fluidized bed reactor used for light olefin cracking and Methanol To Olefin (MTO), which comprises a reactor and a pre-riser; the reactor comprises a dense phase fluidized bed reactor and a dilute phase conveying reactor which are positioned at same axis, the pre-riser and the dilute phase conveying reactor are respectively positioned at upper part and lower part of the dense phase fluidized bed reactor; diameter of the pre-riser is smaller than diameter of the dense phase fluidized bed reactor, the upper part of the pre-riser extends into the dense phase fluidized bed reactor; an upper end port of the pre-riser in the dense phase fluidized bed reactor is sealed, and a perforate is provided on the tube wall of the pre-riser in the dense phase fluidized bed reactor; or the perforate is provided on the upper end of the pre-riser in the dense phase fluidized bed reactor, and a baffle plate is arranged over the perforate. The reactor is capable of increasing gas-solid contact efficiency, the backmixing degree of oil gas and a catalyst is less, and conversion rate of one way of the light olefin cracking and Methanol To Olefin (MTO) reactions can be greatly improved, and the target product micromolecule olefin selectivity can be greatly improved.

Description

technical field [0001] The invention relates to a fluidized bed reactor for light olefin cracking and methanol-to-olefin production, in particular to a dense-phase fluidized-bed reactor with high gas-solid contact efficiency for light olefin cracking and methanol-to-olefin production. Background technique [0002] Butene, pentene and hexene are very good raw materials for catalytic cracking to produce propylene or ethylene and propylene. The cracking of light olefins mentioned here refers to the catalytic cracking of butene, pentene and hexene. The target products of cracking can be Propylene, and also ethylene and propylene. [0003] The catalyst active components used in catalytic cracking are all acidic molecular sieves. The target products ethylene and propylene produced by the cracking of light olefins can easily undergo secondary reactions on acidic molecular sieve materials and be converted into low value-added products such as alkanes. Therefore, as a light olefin c...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J8/24C07C4/06C07C1/20C07C11/02
CPCB01J8/24B01J2208/00548C07C1/20C07C4/06C07C11/02C07C11/06C07C11/04Y02P30/20Y02P30/40
Inventor 李春义
Owner CHINA UNIV OF PETROLEUM (EAST CHINA)
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