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Rectification method in acetic acid synthesis process by low-pressure methanol carbonylation

An oxo, low-pressure technology, applied in the field of rectification, can solve problems such as unreasonable utilization of rectification energy, consumption of water cycle energy, and insufficient utilization

Active Publication Date: 2006-07-19
SOUTHWEST RES & DESIGN INST OF CHEM IND
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] The disadvantage of the above process is that the energy utilization of rectification is unreasonable. The temperature of the steam at the top of the finished product tower is higher than 130°C. The heat is taken away by the circulating water of the condenser, which is not fully utilized, and the energy required for water circulation is also consumed.

Method used

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  • Rectification method in acetic acid synthesis process by low-pressure methanol carbonylation
  • Rectification method in acetic acid synthesis process by low-pressure methanol carbonylation

Examples

Experimental program
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Effect test

Embodiment 1

[0015] Example 1 Light removal tower, dehydration tower and finished product tower are all plate rectification towers

[0016] The vapor phase material flow rate that flasher produces is 68.81t / h, and composition (weight percent, the same below) is: non-condensable steam 1.02%, hydrogen iodide 0.06%, iodomethane 37.98%, methyl acetate 1.55%, water 11.64% , 47.62% acetic acid, 0.13% propionic acid. Light removal tower 1 top pressure 190kPa (absolute pressure, hereinafter the same), reflux ratio promptly enters the liquid flow rate (mol / h) of rectifying section and the ratio of tower top distillate flow rate (mol / h) is 2.0, light removal Column reboiler 4 adds heat 1.633Mw. The top pressure of the dehydration tower 6 is 110kPa, and the reflux ratio is 1.2. The pressure at the top of the product column 9 is 250kPa, the reflux ratio is 3.0, and the heat added to the reboiler 10 of the product column is 12.903Mw. The liquid in the dehydration tower 6 and the top steam in the pro...

Embodiment 2

[0020] Example 2 Light removal tower, dehydration tower and finished product tower are all porcelain corrugated packing towers

[0021] The flow rate of the vapor phase material produced by the flasher is 6.525t / h, and the composition is: 0.98% of non-condensable steam, 0.04% of hydrogen iodide, 37.38% of methyl iodide, 1.61% of methyl acetate, 11.97% of water, 47.9% of acetic acid, propionic acid 0.12%. The top pressure of light removal tower 1 is 190kPa, the reflux ratio is 2.0, and the heat added to reboiler 4 of light removal tower is 0.06Mw. The top pressure of the dehydration tower 6 is 110kPa, and the reflux ratio is 1.4. The pressure at the top of the product column 9 is 200kPa, the reflux ratio is 2.8, and the heat added to the reboiler 10 of the product column is 1.30Mw. The bottom liquid of dehydration tower 6 and the top steam of finished product tower 9 are heat-exchanged in the reboiler-condenser 82, and the liquid of dehydration tower 6 is boiled in the reboil...

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Abstract

The disclosed rectification method in low-pressure oxo synthesis for acetic acid with methanol comprises: feeding the material produced by flash evaporation or evaporation into the dehydrogenation tower, dehydration column and product tower with condensing temperature higher than the boiling temperature of kettle liquor in dehydrogenation tower by turns; using the heat from steam condensation in heat exchange device as the heat resource for dehydrogenation tower. This invention can save almost 50% heating steam and the energy consumed by water circulation in product tower.

Description

technical field [0001] The invention relates to a rectification method in the low-pressure carbonylation process of methanol to acetic acid. Background technique [0002] The rectification process in the existing oxo acetic acid process includes three rectification towers: a light removal tower (also called an initial distillation tower), a dehydration tower (drying tower) and a finished product tower (weight removal tower). Its process is as figure 1 As shown: the vapor phase material produced by the flash evaporator or evaporator enters the light removal tower 1, and after being condensed by the light removal tower condenser 2, it is divided into two liquid phases in the stratifier 3, and the heavy phase returns to the reactor; the light phase A part is returned to the reactor, and a part is refluxed to the top of the light removal tower 1. The liquid in the bottom of the light removal tower 1 is heated by the reboiler 4 of the light removal tower, and the residual liqui...

Claims

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Application Information

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IPC IPC(8): C07C51/12C07C51/44C07C53/08
Inventor 胡文励王晓东曾健廖炯谢经国李煊毛震波陈群文
Owner SOUTHWEST RES & DESIGN INST OF CHEM IND
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