Preparation process for propylene from methanol or dimethyl ether

A technology of dimethyl ether and methanol, which is applied in the field of producing propylene from methanol or dimethyl ether, can solve the problems of high cost and high energy consumption, and achieve the effects of increased yield, shortened separation process, and reduced energy consumption for product gas compression and separation

Active Publication Date: 2015-06-03
PUJING CHEM IND SHA
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] The ethylene separation cycle existing in the existing MTP industrialization unit leads to the problems of high cost and high energy consumption in the separation process

Method used

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  • Preparation process for propylene from methanol or dimethyl ether
  • Preparation process for propylene from methanol or dimethyl ether
  • Preparation process for propylene from methanol or dimethyl ether

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0040] The first reactor is composed of two adiabatic fixed-bed reactors connected in parallel for switching reaction regeneration. In each adiabatic fixed-bed reactor, high-silicon ZSM-5 is used as the catalyst, the catalyst Si / Al ratio is 50, and the specific surface area is 350m 2 / g, pore volume 0.112ml / g. In an adiabatic fixed-bed reactor, methanol and separation system returns to C 4 The above components (ie C 4 The above cycle hydrocarbons) are converted into reaction gases rich in propylene. The feed composition mass ratio of the first reactor: Methanol (as CH 2 Count): water: C 4 The above cycle hydrocarbons=1:10:0.5, the reaction is based on methanol feed, and the weight hourly space velocity of methanol is 1h -1 , the reactant inlet temperature is 550°C, and the reaction pressure is 0.30MPa. The reaction results of the first reactor are shown in Table 1.

[0041] The second reactor is composed of two adiabatic fixed-bed reactors connected in parallel for switc...

Embodiment 2

[0043] The first reactor consists of five adiabatic fixed-bed reactors connected in parallel, four for reaction and one for catalyst regeneration. In each adiabatic fixed-bed reactor, high-silicon ZSM-5 is used as the catalyst, the catalyst Si / Al ratio is 220, and the specific surface area is 350m 2 / g, pore volume 0.112ml / g. In an adiabatic fixed-bed reactor, methanol and C 4 The above higher hydrocarbons are converted into reaction gases rich in propylene. The feed composition mass ratio of the first reactor: dimethyl ether (as CH 2 Count): water: C 4 The above cycle hydrocarbons=1:5:4, the reaction is based on methanol feed, and the weight hourly space velocity of methanol is 3h -1 , the reactant inlet temperature is 460°C, and the reaction pressure is 0.1MPa. The reaction results of the first reactor are shown in Table 1.

[0044] The second reactor is composed of two nearly isothermal tubular fixed-bed reactors connected in parallel, one for reaction and one for cat...

Embodiment 3

[0046] The first reactor is composed of three adiabatic fixed-bed reactors connected in parallel with cold shock of intermediate raw materials, two for reaction and one for regeneration. In each adiabatic fixed-bed reactor, high-silicon ZSM-5 is used as the catalyst, the catalyst Si / Al ratio is 500, and the specific surface area is 350m 2 / g, pore volume 0.112ml / g. In the reactor, methanol and C 4 The above higher hydrocarbons are converted into reaction gases rich in propylene. The reactant inlet temperature is 380°C, the reaction pressure is 0.13MPa, and the feed composition mass ratio of the first reactor is methanol (in the form of CH 2 Count): water: C 4 The above cycle hydrocarbon = 1:0:10, the reaction is based on methanol feed, and the space velocity is 10h -1 . The reaction results of the first reactor are shown in Table 1.

[0047] The second reactor consists of five nearly isothermal tubular fixed-bed reactors connected in parallel, four for reaction and one f...

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Abstract

The invention relates to a preparation process for propylene from methanol or dimethyl ether. The process comprises the following steps: allowing the raw materials consisting of methanol or dimethyl ether, water and above-C4 components returned from a separation system to undergo a reaction in a first reactor so as to produce propylene-rich C1-C10 components which enter into the separation system; separating propylene from the separation system as a product and allowing above-C4 components to return to the reactor; and subjecting C1-C2 components in the separation system to a reaction in a second reactor to produce above-C3 high-carbon substances and returning the above-C3 high-carbon substances to the separation system to promote yield of propylene; wherein selectivity of propylene in the first reactor is greater than 70%, and the yield of propylene after propylene-yield promotion by the second reactor is greater than 75%. Compared with the prior art, the process provided by the invention has the advantages of high selectivity of the product propylene, no need for an ethylene cryogenic fractionation system, low content of C2 and below-C2 components, simplification of the separation system and substantial reduction of energy consumption of the separation system.

Description

technical field [0001] The invention relates to a process for producing propylene from methanol or dimethyl ether. Background technique [0002] Propylene is an important organic chemical raw material, mainly used in the production of polypropylene, acrylonitrile and acrylic acid. At present, propylene is mainly obtained from petroleum raw materials through steam cracking or catalytic cracking, and its price is affected by the price of petroleum. The shortage of petroleum resource reserves and the growing market demand for propylene make it necessary to develop a propylene production process that does not depend on petroleum. At the same time, the domestic methanol production capacity is seriously oversupplied, and the price of methanol is low. The development of methanol to propylene (MTP) technology can use abundant coal or natural gas to produce propylene through methanol, and open up a non-petroleum route propylene production technology, which has broad market prospect...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C11/06C07C1/20
CPCY02P20/52Y02P30/20Y02P30/40
Inventor 吴文章张博计扬
Owner PUJING CHEM IND SHA
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