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Production method of n-butyl acetate

A technology of n-butyl acetate and its production method, which is applied to the preparation of carboxylic acid esters, chemical instruments and methods, and the preparation of organic compounds, and can solve the problems of wasting energy and water resources, high energy consumption, etc., and achieve the reduction of steam consumption and saving Water resources and the effect of reducing equipment investment

Active Publication Date: 2014-05-21
LINYI JINYIMENG BIOTECH
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

In the dehydration refining tower system and the recovery tower system, the energy consumption is high, which occupies a large share in the production cost of n-butyl acetate in industry, and also wastes some precious energy and water resources.

Method used

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  • Production method of n-butyl acetate
  • Production method of n-butyl acetate
  • Production method of n-butyl acetate

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0033] The production method of n-butyl acetate of the present invention comprises following operation steps:

[0034] ①Esterification

[0035] The raw material butanol and acetic acid react in the esterification kettle 1, and the generated n-butyl acetate and water, after vaporization, carry part of the raw materials into the esterification distillation tower 3, and continue the esterification reaction in the esterification distillation tower 3 and undergo distillation. Separation, the ternary azeotrope of n-butyl acetate, butanol and water distilled from the top of the tower is cooled and condensed by the esterification condenser A 4 and the esterification condenser B 5, and then enters the esterification phase separator 6, and the upper layer of crude ester Through the esterification reflux pump 7, part of it is pumped into the esterification distillation tower 3 as a top reflux; the other part is pumped into the dehydration refining tower 8;

[0036] ②.Dehydration and ref...

Embodiment 2

[0044] According to the method and steps of embodiment 1, the difference is:

[0045]①. The gas distilled from the top of the dehydration and refining tower 8 enters the reboiler 17 tube of the recovery tower, exchanges heat with the material in the tube, and then enters the auxiliary heat exchanger 25, exchanges heat with the feed of the dehydration and refining tower 8, and condenses The liquid enters the dehydration and refining tower condenser A (10, and then enters the dehydration and refining tower phase separator 12 for stratification, the upper layer of material is sent to the dehydration and refining tower 8 by the reflux pump 13, and the lower layer of material is sent to the waste water tank for collection ; Dehydration refining tower 8 tower kettle material is pumped into n-butyl acetate finished product condenser 15 by n-butyl acetate finished product pump 14, after cooling, obtains ethyl acetate finished product.

[0046] ②. The operating conditions of the dehydr...

Embodiment 3

[0050] According to the method and steps of embodiment 1, the difference is:

[0051] ①. The gas distilled from the top of the dehydration and refining tower 8 enters the reboiler 17 tube of the recovery tower, and after exchanging heat with the material in the tube, it enters the auxiliary heat exchanger 25, and after exchanging heat with the feed of the dehydration and refining tower 8, no further After being further cooled and condensed by the top condenser of the dehydration refining tower, it directly enters the phase separator 12 of the dehydration refining tower for stratification.

[0052] ②. The operating conditions of the dehydration refining tower 8 are as follows:

[0053]

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Abstract

The invention relates to a production method of n-butyl acetate, belonging to synthesis of acetates of unitary hydroxyl compounds. The production method comprises an esterification distillation operating system, a dehydration refinement operating system and a recycling distillation operating system. The invention is characterized in that heat carried by tower top distillate gas of a dehydration refinement tower (8) is used as a heat source of a recovery tower reboiler (17); the tower top distillate gas firstly enters among tubes of the recovery tower reboiler (17), exchanges heat with the material in the tubes to get cooled, is further cooled and condensed through a dehydration refinement tower condenser A (10), and enters a phase splitter for phase splitting; and the organic phase material is totally sent into the top of the dehydration refinement tower (8) and totally refluxed. The method has the advantages of equipment investment saving, lower production cost, lower energy consumption and water resource saving. The steam consumption in the dehydration rectification process is lowered by 10%, 0.2 ton of steam can be saved per ton of products, and 100 cubic meters of tower top condensation water is saved every hour.

Description

technical field [0001] The present invention is a kind of production method of n-butyl acetate. Synthesis of acetate esters belonging to monohydric hydroxy compounds. Background technique [0002] In the process of producing n-butyl acetate by esterification, acetic acid and n-butanol react in the esterification tank to generate n-butyl acetate, which is initially rectified in the esterification tower, and then separated by a phase separator, and the organic phase is sent to The dehydration refining tower system, after dehydration and dealcoholization, obtains n-butyl acetate as a finished product; the water phase passes through the recovery tower system, recovers n-butanol and n-butyl acetate in it, and sends it to the esterification tower system for recycling. In the dehydration refining tower system and the recovery tower system, the energy consumption is high, which occupies a large share in the production cost of n-butyl acetate in industry, and also wastes some precio...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C69/14C07C67/08C07C67/54
Inventor 张超张立省马晓丽何晓芳张金玲
Owner LINYI JINYIMENG BIOTECH
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