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Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material

A technology of dimethyl carbonate and dimethyl oxalate, applied in the purification/separation of carbonate/haloformate, organic chemistry, etc., can solve the problems of high energy consumption and complicated operation

Active Publication Date: 2016-01-27
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0013] The technical problem to be solved by the present invention is that the prior art has the problems of complicated operation and high energy consumption, and a new method for separating low-concentration dimethyl carbonate in the process of synthesizing dimethyl oxalate from coal-based synthesis gas is provided

Method used

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  • Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material
  • Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material
  • Method for separating low-concentration dimethyl carbonate during process of synthesizing dimethyl oxalate with coal-based synthetic gas as raw material

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0030]The crude methanol solution 1 after the separation of DMO enters the light removal tower T-101, and the top gas 2 of the light removal tower enters the light removal tower condenser E-102. After the light tower kettle pump P-101 is pressurized, 6 enters the atmospheric tower, and the top gas 7 of the atmospheric tower enters the atmospheric tower condenser E-102. Pressurized tower, atmospheric tower tank liquid is pressurized by atmospheric tower tank pump P-102 12 as methanol product and recycled in the synthesis gas to ethylene glycol plant. When the device is started, all the top gas 13 of the pressurization tower is condensed by the start-up condenser E-106A of the pressurization tower and enters the reflux tank D-101 of the pressurization tower. Part of the heat is exchanged with the reboiler E-101 of the light removal tower through the pipeline 16 and then returned to the reflux tank D-101 of the pressurization tower, and the remaining part of the top gas 13 of the...

Embodiment 2

[0038] Different from [Example 1], the theoretical plate number of the atmospheric column is 55, the operating pressure at the top of the tower is 40kPaG, and the temperature at the top of the tower is 72°C; the operating pressure of the tower still is 75kPaG, the temperature of the tower still is 79°C, for 12. The theoretical plate number of the pressurized tower is 35, the operating pressure at the top of the tower is 1000kPaG, and the temperature at the top of the tower is 137°C;

[0039] Among them, the main logistics components are as follows:

[0040]

[0041] Under normal operating conditions, the reboiler and condenser loads of each column are as follows:

[0042] Load, MW T-101 T-102 T-103 reboiler - 29.935 5.732 condenser 3.756 31.352 1.274

[0043] Among them, 74.6% of T-103 overhead gas is supplied to T-101 reboiler as a heat source, and the load of T-103 overhead condenser is reduced by 74.6%.

Embodiment 3

[0045] Different from [Example 1], the feed composition of crude methanol solution 1 is different, the number of theoretical plates in the atmospheric column is 60, the operating pressure at the top of the tower is 70kPaG, and the temperature at the top of the tower is 78°C; the operating pressure at the bottom of the tower is 115kPaG, The temperature of the tower kettle is 85°C, and the reflux ratio is 10. The pressurized tower has 50 theoretical plates, the operating pressure at the top of the tower is 1150kPaG, and the temperature at the top of the tower is 146°C;

[0046] Among them, the main logistics components are as follows:

[0047]

[0048] Under normal operating conditions, the reboiler and condenser loads of each column are as follows:

[0049] Load, MW T-101 T-102 T-103 reboiler - 31.542 7.685 condenser 3.487 32.724 2.537

[0050] Among them, 62.6% of T-103 overhead gas is supplied to T-101 reboiler as a heat source, while the...

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Abstract

The invention relates to a method for separating low-concentration dimethyl carbonate during a process of synthesizing dimethyl oxalate with coal-based synthetic gas as a raw material. The invention mainly aims at solving the problems of complicated operation and high energy consumption of prior arts. According to the invention, a crude methanol solution containing small amounts of dimethyl carbonate and methyl formate is delivered to a light component removing column, such that methyl formate is removed; the obtained material is delivered to a double-column process composed of atmospheric column-pressurized column, such that dimethyl carbonate is removed through separation, and methanol can be recovered and recycled. A large proportion of pressurized column overhead gas is adopted as a heat source for a light component removing column kettle reboiler. With the technical scheme, the problems are well solved. The method can be used in ethylene glycol industrial productions.

Description

technical field [0001] The invention relates to a method for separating low-concentration dimethyl carbonate in the process of synthesizing dimethyl oxalate with coal-based synthesis gas as a raw material. Background technique [0002] In the process of synthesizing dimethyl oxalate, methyl nitrite and CO undergo a gas-phase catalytic coupling reaction on the catalyst to generate dimethyl oxalate DMO, while there is dimethyl carbonate DMC generated by side reactions. The reaction equation is as follows: [0003] 2CH 3 ONO+2CO→(COOCH 3 ) 2 +2NO [0004] The main side effects are: [0005] 2CH 3 ONO+2CO→CO(OCH 3 ) 2 +2NO [0006] The by-product methyl formate (MF) is also formed in the presence of hydrogen. The reaction equation is as follows: [0007] CH 3 ONO + 2 CO + 1 2 H 2 → CHOOC ...

Claims

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Application Information

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IPC IPC(8): C07C69/96C07C68/08
Inventor 贺来宾杨卫胜胡松
Owner CHINA PETROLEUM & CHEM CORP
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