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Continuous process for preparing hydrocarbon products through methanol transformation without standby reactor

A technology for the conversion of hydrocarbon products and methanol, which is applied in the continuous process field, can solve the problems of cumbersome operation of regeneration system control and actuators, increased investment in automatic control parts, and lower reliability of equipment operation, so as to simplify the automatic control part and improve stability performance and reliability, and the effect of reducing equipment investment

Active Publication Date: 2010-08-25
SHANXI INST OF COAL CHEM CHINESE ACAD OF SCI +2
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0006] 1. Since the standby reactor is always in the regeneration state or standby state, its production capacity cannot be exerted, resulting in waste of equipment production capacity and increased equipment investment;
[0007] 2. All reactors, including online reactors and standby reactors, need to set up catalyst regeneration process control and actuators separately, and the investment in the automatic control part increases;
[0008] 3. Reactors are regenerated one by one, and the control and actuators of the regeneration system are cumbersome to operate, which reduces the reliability of equipment operation

Method used

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  • Continuous process for preparing hydrocarbon products through methanol transformation without standby reactor
  • Continuous process for preparing hydrocarbon products through methanol transformation without standby reactor

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Embodiment 1

[0022] Embodiment 1 takes the one-step process of methanol conversion to gasoline in a fixed-bed adiabatic reactor as an example, and adopts the process flow of the accompanying drawing. The number of the first group of reactors 6 and the number of the second group of reactors 7 are both 2, and each reactor is filled with 100 kg of methanol conversion to gasoline catalyst (ZSM-5 molecular sieve catalyst). The reaction pressure was 1.6 MPa, the inlet temperature of each reactor was 320°C, and the outlet temperature was 410°C. The specific implementation steps are as follows.

[0023] 1. Turn on the first group of reactors

[0024] As shown in the process flow chart, when starting for the first time, open the reaction material inlet valve (4) and the reaction material outlet valve (8) of the first group of reactors (6), and close the reaction material inlet valve of the second group of reactors (7) (5), the reaction material outlet valve (9), close the valves (11), (12), (13),...

Embodiment 2

[0040] Embodiment 2 takes methanol conversion to produce LPG as an example. Adopt the process flow shown in the accompanying drawing. The number of the first group of reactors 6 and the second group of reactors 7 are 4 units, and each reactor is filled with 50kg of ZSM-5 molecular sieve catalyst for producing LPG from methanol conversion, and the total amount of catalyst loading is 400kg. The methanol flow rate is 800kg / h, the system pressure is 1.0MPa, the inlet temperature of each reactor is 380°C, and the outlet temperature of each reactor is 510°C. Under the condition that reactor 6 and reactor 7 work simultaneously, the mass space velocity of methanol is 2.0h -1 , when one of the catalysts is in the regeneration state, relative to the working catalyst, the methanol mass space velocity is 4.0h -1 . Concrete implementation steps are with embodiment 1.

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Abstract

The invention discloses a continuous process for preparing hydrocarbon products through methanol transformation without standby reactor. Two groups of reactors are arranged; the first group reactor works first, when a catalyst in the first group of reactor reaches metaphase of lifetime one way, the second group of reactor is started, so that the two groups of reactors are in the simultaneous working state and respectively bear 50 percent of reaction load; when the catalyst in the first group of reactor reaches last phase of the lifetime one way, a catalyst in the second group of reactor is positioned in the metaphase of lifetime one way, and at the moment, the total 100 percent of reaction load is transferred to the second group of reactor and the catalyst in the first group of reactor is regenerated; after the catalyst in the first group of reactor is regenerated, the first group of reactor works, and the two groups of reactors respectively bear 50 percent of reaction load; when the catalyst in the second group of reactor reaches the last phase of the lifetime one way, the catalyst in the first group of reactor is positioned in the metaphase of the lifetime one way, and at the moment, the total 100 percent of reaction load is transferred to the first group of reactor and the catalyst in the second group of reactor is regenerated; the process is repeated so as to realize reaction process continuity under the condition of no standby reactor. The continuous process has the advantages of not needing arranging the standby reactor, simplifying process flow, reducing equipment investment and improving system operation stability and reliability.

Description

technical field [0001] The invention belongs to a continuous process for producing hydrocarbon products by converting methanol, in particular to a continuous process for producing hydrocarbon products by converting methanol without a standby reactor. Background technique [0002] The conversion of methanol to produce hydrocarbons is an important chemical reaction, such as the conversion of methanol to gasoline (the MTG technology of Exxon-Mobil Company, the Shanxi Institute of Coal Chemistry, Chinese Academy of Sciences, Saiding Engineering Company, and Yunnan Coal Chemical Industry Group Co., Ltd. Bed adiabatic reactor one-step methanol conversion to gasoline technology), methanol conversion to propylene (MTP technology of Lurgi company, FMTP technology of Tsinghua University), methanol conversion to olefins (MTO technology of UOP company, DMTO technology of Dalian Institute of Chemical Physics, Chinese Academy of Sciences ), and methanol conversion to aromatics (MTA techno...

Claims

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Application Information

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IPC IPC(8): C07C1/20
CPCY02P20/52Y02P20/584
Inventor 李文怀张庆庚王磊胡津仙张侃张建利方勇潘国平普煜李党
Owner SHANXI INST OF COAL CHEM CHINESE ACAD OF SCI
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