Multi-stage serial fluidized bed reactor and method for methanol to olefins

A fluidized bed reactor, methanol to olefins technology, applied in the direction of hydrocarbon production from oxygen-containing organic compounds, organic chemistry, chemical recovery, etc., can solve the problems of different reactor sizes, temperatures, loads, and limited reaction conditions , to achieve the effect of narrow distribution of carbon deposition, narrow distribution of residence time, and reduction of entrainment

Inactive Publication Date: 2017-01-18
ZHEJIANG UNIV +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

However, the MTO multi-stage reactor introduced in the current patent literature is limited to the riser reactor and fast fluidized bed reactor in addition to the reactor type, and the consideration of the reaction conditions is also very limited. The size, temperature and load of different reactors are different. no discrimination

Method used

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  • Multi-stage serial fluidized bed reactor and method for methanol to olefins
  • Multi-stage serial fluidized bed reactor and method for methanol to olefins
  • Multi-stage serial fluidized bed reactor and method for methanol to olefins

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Embodiment 1

[0046] The results for single-stage reactors are considered first, as a comparison for subsequent consideration of multi-stage reactors. figure 2 Shown is a pilot-scale single fluidized bed reactor with its accessories. The diameter of the reactor is 0.26m, and the operating gas velocity is 0.6m / s, which belongs to the type of turbulent fluidized bed. The mass flow rate of the methanol feed is 41.5kg / h, the water content of the feed is 20%, the catalyst loading is 10.4kg, the reaction temperature is 480°C, the pressure is 0.1MP, and the average residence time of the catalyst in the reactor is 45min. The SAPO-34 catalyst used is a DMTO catalyst produced by Dalian Institute of Chemical Physics, with a specific surface area of ​​263m 2 / g, average particle size 83μm, particle density 1220kg / m 3 . The raw methanol aqueous solution all enters the reactor 16 through the feed channel 5, and the reacted outlet material enters the subsequent olefin separation device 19 through the ...

Embodiment 2

[0050] use image 3 In the two-stage gas-solid co-flow reactor shown, the size of the two reactors is the same, the catalyst loading of each reactor is half of that of the single-stage reactor, and the gas velocity is still the same as that of the single-stage reactor, all of which belong to turbulent fluidization bed type. The raw methanol aqueous solution enters the first-stage reactor 16 through the feed channel 5, and the reacted outlet material enters the second-stage reactor 17 through the gas outlet 6 and the feed channel 3 to continue the reaction, and the reacted outlet material passes through the gas outlet 4 Enter the subsequent olefin separation device 19, after separation, the products ethylene and propylene are obtained from the outlet 13, and other by-products are obtained from the outlet 14. The fresh catalyst output from the regenerator 15 enters the first-stage reactor 16 through the circulation channel 9, where pre-coking is performed and the methanol feed is...

Embodiment 3

[0054] use Figure 4 In the two-stage gas-solid countercurrent reactor shown, the size and type of the reactor are still the same as in Example 2, except that the gas-solid countercurrent contact is adopted. The operating conditions are the same as in Table 2. Raw methanol aqueous solution all enters the second-stage reactor 17 through the feed channel 3, and the reacted outlet material enters the first-stage reactor 16 through the gas outlet 4 and the feed channel 5 to continue the reaction. The exported material enters the subsequent olefin separation device 19 through the gas outlet 6, and after separation, the products ethylene and propylene are obtained from the outlet 13, and other by-products are obtained from the outlet 14. The fresh catalyst output from the regenerator 15 enters the first-stage reactor 16 through the circulation channel 9, performs pre-coking and fully converts the remaining methanol, and the pre-coke catalyst output from the first-stage reactor 16 en...

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Abstract

The invention discloses a three-stage series fluidized bed reactor for methanol-to-olefin reaction and a method of preparing olefin by the reactor. The reaction product and unreacted methanol are separated from a catalyst and then enter a next stage reactor for further reaction. The catalyst flows continuously in the three-stage reactor, compared with a single stage fluidized bed reactor, the carbon deposit distribution is more uniform, and the production capacity of the unit catalyst is effectively enhanced. The three reactors are all operated under respective optimal reaction temperature, gas-solid counter-current operation makes most of methanol react on the catalyst of pre-deposited carbon, and the selectivity of low carbon olefin is enhanced. Compared with a single-stage reactor, the selectivity of low carbon olefin is increased by 0.9%, and the single-pass production capacity of the unit catalyst is increased by 31.1%.

Description

technical field [0001] The invention relates to the field of coal chemical production, in particular to a multi-stage serial fluidized bed reactor for methanol-to-olefin reaction and a method for preparing olefins using the reactor. Background technique [0002] Ethylene and propylene are basic chemical raw materials in the chemical industry. The traditional production method uses petroleum as raw material to obtain low-carbon olefins by cracking high-carbon hydrocarbons and dehydrogenating low-carbon alkanes. The method of producing ethylene and propylene from methanol (MTO) developed in recent years has been industrialized, opening up a new way for the production of bulk petrochemical products from coal. [0003] The catalyst used in methanol-to-olefins is SAPO-34 molecular sieve. The preparation method, use conditions and performance indicators of this catalyst are described in many patents and documents, such as CN 1088483A, CN 1096496A. At present, several sets of MTO...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C1/20C07C11/04C07C11/06
CPCY02P20/584Y02P30/20Y02P30/40
Inventor 李希应磊叶茂成有为王丽军
Owner ZHEJIANG UNIV
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