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An energy recovery method for the process of producing propylene from oxygen-containing compounds

An energy recovery and compound technology, which is applied in the field of propylene production, can solve the problems of large heating furnace load, low energy utilization rate, and low overall energy efficiency level of the process, so as to deepen the heat exchange depth, improve the energy efficiency level of the process, and save energy. consumption effect

Inactive Publication Date: 2016-06-29
ZHEJIANG UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0007] The technical problem solved by the present invention is that in the prior art, the energy utilization rate of the propylene product produced from oxygenated compounds is not high in the post-treatment stage, the reactant stream needs to be heated by a heating furnace before entering the reactor and the load of the heating furnace is too large, and the overall energy efficiency of the process is low. The problem is not high, and a new method for energy recovery of oxygenate to propylene process is provided

Method used

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  • An energy recovery method for the process of producing propylene from oxygen-containing compounds

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Embodiment 1

[0023] In this embodiment, the feed is industrial methanol with a purity of 99.5%, and the methanol feed WHSV=2.0h -1 , using as figure 1 The process flow shown. The gas temperature at the inlet of reactor 5 is 450°C, the temperature of the reaction product after being compressed by the compressor is 600°C, and the pressure is 0.70MPa in gauge pressure. ℃, and then pass through the two-stage heat recovery unit of the methanol vaporizer and the circulating water preheater respectively. The temperature flowing out of the circulating water preheater is 130 ℃, and enters the air cooler to cool down to 30 ℃, and finally enters the phase separator to separate oil and water , gas three-phase. The water content in the outlet gas hydrocarbon product is 0.2wt%, and the water content in the oil phase product is 0.6wt%.

[0024] Through this scheme, the stream flowing out of the pre-reactor 3 is directly heated to 450° C. through a heat exchange to reach the reaction temperature of the...

Embodiment 2

[0028] In this embodiment, the feed is industrial methanol with a purity of 99.5%, and the methanol feed WHSV=1.0h -1 , using as figure 1 The process flow shown. The gas temperature at the inlet of reactor 5 is 400°C, the temperature of the reaction product after being compressed by the compressor is 550°C, and the pressure is 0.60MPa in gauge pressure. ℃, and then pass through the two-stage heat recovery unit of the methanol vaporizer and the circulating water preheater respectively. The temperature flowing out of the circulating water preheater is 110 ℃, and enters the air cooler to cool down to 40 ℃, and finally enters the phase separator to separate oil and water , gas three-phase. The water content in the outlet gas hydrocarbon product is 0.3wt%, and the water content in the oil phase product is 0.7wt%.

[0029] Through this solution, the stream flowing out of the pre-reactor 3 is directly heated to 400° C. through a heat exchange to reach the reaction temperature of t...

Embodiment 3

[0033] In this embodiment, the feed is industrial methanol with a purity of 99.5%, and the methanol feed WHSV=2.0h -1 , using as figure 1The process flow shown. The gas temperature at the inlet of reactor 5 is 380°C, the temperature of the reaction product after being compressed by the compressor is 530°C, and the pressure is 0.55MPa in gauge pressure. ℃, and then pass through the two-stage heat recovery unit of the methanol vaporizer and the circulating water preheater respectively. The temperature flowing out of the circulating water preheater is 100 ℃, and enters the air cooler to cool down to 40 ℃, and finally enters the phase separator to separate oil and water , gas three-phase. The water content in the outlet gas hydrocarbon product is 0.35wt%, and the water content in the oil phase product is 0.72wt%.

[0034] Through this solution, the stream flowing out of the pre-reactor 3 is directly heated to 380° C. through a heat exchange to reach the reaction temperature of ...

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Abstract

The invention discloses an energy recycling method for a process for preparing propylene from oxygenated compounds, for mainly solving the problems that in the prior art, a heating furnace is high in heat load, low in heat exchange depth and low in efficiency level. The adopted technical scheme comprises the following steps: (1) desorbing micromolecule organic acid from an oxygenated compound prepared propylene reactor outlet product by using a deacidification reactor, so as to obtain a high temperature material flow I; (2) compressing and heating the high temperature material flow I, so as to obtain a high temperature material flow II; and (3) sequentially feeding the high temperature material flow II into a raw material gas preheater, a methanol gasifier and a circulation water preheater for respectively preheating a raw material gas, gasifying methanol and preheating circulation water. The method saves the energy consumption of a heating furnace of a conventional process and improves the process efficacy level, and meanwhile as the compression section of the product is brought forward, a better effect is achieved in phase separation, and the content of water in gas phase and oil phase is greatly reduced.

Description

technical field [0001] The invention belongs to the field of propylene production, and in particular relates to an energy recovery method for the process of producing propylene from oxygen-containing compounds. Background technique [0002] Propylene is an important basic chemical raw material in the modern chemical industry, and 95% of its total comes from naphtha steam cracking co-production and fluid catalytic cracking (FCC) by-product. Affected by the continuous rise in global crude oil prices and the shift of ethylene raw materials to light hydrocarbons such as ethane, the global propylene demand gap continues to grow. At the same time, the methanol-to-propylene (MTP) process, which uses coal-based methanol or natural gas / shale gas-based methanol as raw material to produce propylene, is increasingly favored by various countries. In view of my country's "coal-rich, oil-deficient, and gas-poor" energy structure, the development of MTP technology with coal-based methanol ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C1/20C07C11/06
CPCY02P20/10Y02P20/50
Inventor 廖祖维冯翔蒋斌波王靖岱阳永荣黄正梁严丽霞蒋云涛陆飞鹏
Owner ZHEJIANG UNIV
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