Method for treating coarse liquor gas during differential pressure distillation

A treatment method and technology for alcohol gas, which are applied in chemical instruments and methods, preparation of organic compounds, separation/purification of hydroxyl compounds, etc., can solve problems such as unutilized heat energy and affect the operation stability of the subsequent process of the crude distillation column. , to save energy, avoid flooding, and improve stability.

CN102126922AInactive Publication Date: 2011-07-20CHINA PETROCHEMICAL CORP +1
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Patent Information

Authority / Receiving Office
CN · China
Patent Type
Applications(China)
Current Assignee / Owner
Publication Date
2011-07-20
Estimated Expiration
Not applicable · inactive patent

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Abstract

The invention relates to a method for treating coarse liquor gas during differential pressure distillation, which mainly solves the problems of no utilization of heat energy contained in the coarse liquor gas and the influence of non-condensable gas in the coarse liquor gas on operation stability of subsequent processes of a coarse distillation tower in the prior art. The method comprises the following steps of: a) adding fermentation mash into the upper part of the coarse distillation tower and performing coarse distillation to obtain the coarse liquor gas on the top of the tower and waste mash in the kettle of the tower; and b) introducing the coarse liquor gas into at least two stages of tandem heat exchangers sequentially, condensing stage by stage to obtain coarse liquor condensed liquid, performing a subsequent rectification process on the condensed liquid, and exhausting the non-condensable gas outside or performing subsequent working section treatment on the non-condensable gas. By the technical scheme, the problems are preferably solved; and the method can be applied in the industrial production process for preparing azeotropy ethanol by differential pressure distillation.
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Description

Technical field

[0001] The invention relates to a method for processing crude wine gas in differential pressure distillation. Background technique

[0002] With the increasing shortage of petroleum resources, the deterioration of the natural environment is in urgent need of improvement. Fuel ethanol, as an energy source that has little environmental pollution and can replace petroleum, has attracted the attention of all countries.

[0003] At present, the process of producing fuel ethanol from fermented mash mostly adopts a two-column or three-column distillation method. The document CN1644703A provides a fuel ethanol production method, which uses a two-tower process of a mash tower and a dehydration tower to produce fuel ethanol. The two towers of this process are operated under differential pressure, and the crude wine gas enters the dehydration tower in the gas phase. The document CN101085717A provides a process method for ethanol rectification using a three-tower heat integra...

Examples

Embodiment 1

[0018] use figure 1 In the process shown, the fermentation mash with an ethanol content of 9% by weight is preheated by the primary heat exchanger 7 and then enters the upper part of the crude distillation tower. After the crude distillation, the ethanol content at the top of the crude distillation tower is 48% by weight. The crude alcoholic gas is obtained in the tower kettle to obtain a waste mash with an ethanol content of less than 0.005% by weight. The crude wine gas enters the first-stage heat exchanger 7, the second-stage heat exchanger 8 and the third-stage heat exchanger 9 successively, and obtains the crude wine condensate after being condensed step by step. The crude wine condensate enters the upper part of the distillation tower in the subsequent process ; Non-condensable gas is discharged outside.

[0019] The operating conditions of the crude distillation column are: the number of trays is 26, the feed position is the second tray from top to bottom, the operating pr...

Embodiment 2

[0022] According to the steps of [Example 1], only the fermented mash enters the upper part of the crude distillation tower without preheating.

[0023] The operating conditions of the rough distillation column are: the number of trays is 26, the feed position is the second tray from top to bottom, the operating pressure is 30kPa, the top temperature is 54°C, and the bottom temperature is 76°C. The outlet temperature of the first-stage heat exchanger is 33°C, the outlet temperature of the second-stage heat exchanger is 20°C, and the outlet temperature of the third-stage heat exchanger is 16°C. The operating conditions of the rectification tower are: the number of trays is 50, the feeding position is the 48th tray from top to bottom, the operating pressure is 100kPa, the top temperature is 78°C, and the bottom temperature is 86°C.

[0024] After the device runs for 300 days, the three-stage heat exchanger recovers a total of 8×10 heat 5 kJ, at the same time, the rectification tower ...

Embodiment 3

[0026] According to the steps of [Example 1], but the operating conditions of the crude distillation column are: the number of trays is 26, the feed position is the second tray from top to bottom, the operating pressure is 60kPa, and the top temperature is 69°C, The temperature of the tower kettle is 90°C. The outlet temperature of the first-stage heat exchanger is 37.5°C, the outlet temperature of the second-stage heat exchanger is 25°C, and the outlet temperature of the third-stage heat exchanger is 18.3°C. The operating conditions of the distillation tower are: the number of trays is 50, the feed position is the 48th tray from top to bottom, the operating pressure is 170kPa, the top temperature is 92°C, and the bottom temperature is 99°C.

[0027] After 300 days of operation, the three-stage heat exchanger recovers a total of 6.9×10 heat 5 kJ, at the same time, the rectification tower has no flooding phenomenon, and the operation is stable.