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Recovery method of pressure energy in methanol to olefins unit

A technology of methanol to olefins and recovery methods, which is applied in separation methods, chemical instruments and methods, and hydrocarbon production from oxygen-containing organic compounds, etc., can solve the problems of high operating energy consumption and high power and electricity costs.

Active Publication Date: 2021-05-18
SINOPEC SHANGHAI ENG +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0006] The technical problem to be solved by the present invention is the problem of high power and electricity costs and high energy consumption in operation in the prior art. It provides a new method for recovering pressure energy of a methanol-to-olefins plant, which has the advantages of low power and electricity costs and low energy consumption in operation

Method used

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  • Recovery method of pressure energy in methanol to olefins unit
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  • Recovery method of pressure energy in methanol to olefins unit

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Embodiment 1

[0033] Taking a methanol-to-olefins plant with a production scale of 1.8 million tons per year as an example, a method for recovering pressure energy of a methanol-to-olefins plant according to the present invention is adopted, and the composition of the product gas generated by the methanol-to-olefins reaction is shown in Table 2.

[0034] Table 2 List of product gas composition of methanol to olefins unit

[0035] component name hydrogen methane Vinyl ethane Propylene propane carbon four water carbon dioxide total Yield / mol% 2.81 3.64 46.51 0.87 30.16 1.95 8.19 5.81 0.06 100.00

[0036] Such as figure 1 As shown, the process flow is as follows: the product gas 11 from the external methanol-to-olefins unit enters the bottom of the absorption tower 1, and at the same time, the low-temperature lean liquid absorbent 23 after the temperature is lowered and the pressure is increased enters the top of the absorption tower 1, and in t...

Embodiment 2

[0040] Same as [Example 1], the production scale is still 1.8 million tons / year methanol-to-olefins plant, only the process parameters are changed as follows: the mass ratio range of ethylene / propylene in the product gas of the methanol-to-olefins plant is E / P=1.0:1.0. The operating pressure of the absorption tower 1 is 1.5MPa, the operating temperature at the top of the tower is 55°C, and the operating temperature at the bottom of the tower is 58°C. The absorption tower 1 uses monoethanolamine MEA with a mole fraction of 15% as the absorbent. The operating pressure of the desorption tower 6 is 0.1 MPa, the operating temperature at the top of the tower is 100°C, and the operating temperature at the bottom of the tower is 104°C. The desorption tower 6 adopts external direct steam to operate with an operating pressure of 0.2MPa and an operating temperature of 140°C. Pressure recovery device 3 The inlet operating pressure of the decompression end is 1.5MPa, the outlet operating ...

Embodiment 3

[0043] Same as [Example 1], the production scale is still 1.8 million tons / year methanol-to-olefins plant, only the process parameters are changed as follows: the mass ratio range of ethylene / propylene in the product gas of the methanol-to-olefins plant is E / P=1.0:1.0. The operating pressure of absorption tower 1 is 2.5MPa, the operating temperature at the top of the tower is 72°C, and the operating temperature at the bottom of the tower is 75°C. The absorption tower 1 uses 35% diethanolamine DEA as the absorbent. The operating pressure of the desorption tower 6 is 1.1 MPa, the operating temperature at the top of the tower is 115° C., and the operating temperature at the bottom of the tower is 119° C. The desorption tower 6 adopts external direct steam with operating pressure of 1.2MPa and operating temperature of 208°C. Pressure recovery device 3 The inlet operating pressure of the decompression end is 2.5MPa, the outlet operating pressure is 1.4MPa; the inlet operating pres...

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Abstract

The invention relates to a method for recovering the pressure energy of a methanol-to-olefins device, which mainly solves the problems of high power and electricity costs and large operating energy consumption in the prior art. The present invention adopts a method for recovering the pressure energy of the methanol-to-olefins plant, and adds a pressure recovery device between the absorption tower and the desorption tower to convert the high-pressure liquid-rich absorbent at the top of the absorption tower into a low-pressure liquid-rich absorbent, and simultaneously desorb the The low-pressure lean liquid absorbent at the bottom of the tower is transformed into a high-pressure lean liquid absorbent, thereby saving electricity costs and externally supplied energy. The technical solution solves the above problems well, and can be used in methanol-to-olefins units.

Description

technical field [0001] The invention relates to a method for recovering pressure energy of a methanol-to-olefins device. Background technique [0002] The methanol-to-olefins MTO unit is a "bridge" for the combination of traditional coal chemical industry and traditional petrochemical industry. It plays a role of "connecting the past and ushering in the future" in the coal-to-olefins project, and is also the most critical and core process production device in the coal-to-olefins project. The methanol-to-olefins unit consists of a catalytic reaction unit and an olefin separation unit. Methanol is converted into ethylene, propylene and other target products through the catalytic reaction unit. The product gas composed of these target products contains trace carbon dioxide components and needs to be removed in the olefin separation unit. . Since the olefin separation unit is similar to the mature ethylene plant separation unit at home and abroad, the carbon dioxide component i...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): B01D53/14C07C1/20C07C11/04C07C11/06
CPCB01D53/1425B01D53/1475B01D2252/20484B01D2252/20489C07C1/20C07C11/04C07C11/06Y02P20/151Y02P20/50Y02P30/20Y02P30/40Y02C20/40
Inventor 李真泽吴德荣何琨
Owner SINOPEC SHANGHAI ENG