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Method for preparing ketene compound

A technology for compounds and ketenes, which is applied in the field of preparing ketene compounds, can solve the problems of low relative conversion rate and yield index, low single-pass yield of ketene compounds, limited popularization and application, etc., and achieves low production cost, The effect of less carbon deposition and less pyrolysis by-products

Active Publication Date: 2019-08-09
ZHEJIANG HENGYI PETROCHEMICAL RES INST CO LTD
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  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

However, in the thermal cracking process of isobutyric acid and isobutyric anhydride, the relevant conversion rate and yield index are low, which limits the popularization and application of this technology
[0005] In summary, although researchers in the industry have continuously improved and innovated the high-temperature pyrolysis technology of fatty acids or fatty acid anhydrides (development of new catalysts, shortening of residence time, direct polymerization of DMK, etc.), they still have not solved the problem of enone compounds. Problems such as by-products and carbon deposition caused by cracking, so the single-pass yield of enone compounds is low and the production cost is high

Method used

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  • Method for preparing ketene compound

Examples

Experimental program
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Effect test

Embodiment 1

[0059] like figure 1 As shown, acetic acid (purity 99%), nitrogen, light hydrocarbons (methane: ethylene mass ratio=6:4) enter preheater 1 after mixing with the mass ratio of 70% / 20% / 10%, the mass of the mixture The flow rate is 5.71g / min. After being heated and vaporized by the preheater 1, the temperature rises to 350°C, and then passes into the high-temperature cracking reactor 2, where the reaction temperature is 750°C and the reaction pressure is 25kPa. After the reaction, the mixed gas passes through the secondary condenser 3 to liquefy the heavy components, and after condensation, the gas-liquid mixture enters the gas-liquid separator 4 to separate the liquid phase and transfer it to the condensate storage tank 5, while the gas phase rich in ketene (DK) Points enter the absorption tower 6 from the bottom. The operating temperature of the absorption tower is 110°C, the pressure is 2atm, the absorbent is isobutyl isobutyrate, and the flow rate is 5mL / min. After two-phas...

Embodiment 2

[0063] like figure 1 As shown, isobutyric acid (purity 99%), nitrogen, light hydrocarbons (ethane: propylene mass ratio = 6:4) are mixed with 70% / 17.44% / 12.56% of the mass ratio and then enter the preheater 1, The mass flow rate of the mixture is 5.43g / min. After being heated and vaporized by the preheater 1, the temperature rises to 330°C, and then passes into the high temperature cracking reactor 2, wherein the reaction temperature is 550°C and the reaction pressure is 40kPa. After the reaction, the mixed gas passes through the secondary condenser 3 to liquefy the heavy components. After condensation, the gas-liquid mixture enters the gas-liquid separator 4 to separate the liquid phase and transfer it to the condensate storage tank 5, which is rich in dimethyl ketene (DMK) The gas phase components enter the absorption tower 6 from the bottom. The operating temperature of the absorption tower is 120°C, the pressure is 3atm, the absorbent is dimethyl 1,4-cyclohexyldicarboxyla...

Embodiment 3

[0067] like figure 1As shown, isobutyric anhydride (purity 98%), nitrogen, low-carbon hydrocarbons (ethane: propylene: propane mass ratio = 4:3:3) are mixed at a mass ratio of 83.3% / 11.7% / 5% and then enter the pre- Heater 1, the mass flow rate of the mixture is 6.0g / min, the temperature rises to 330°C after being heated and vaporized by preheater 1, and then passes into high-temperature cracking reactor 2, where the reaction temperature is 450°C and the reaction pressure is 72kPa . After the reaction, the mixed gas passes through the secondary condenser 3 to liquefy the heavy components. After condensation, the gas-liquid mixture enters the gas-liquid separator 4 to separate the liquid phase and transfer it to the condensate storage tank 5, which is rich in dimethyl ketene (DMK) The gas phase components enter the absorption tower 6 from the bottom. The operating temperature of the absorption tower is 117°C, the pressure is 3atm, the absorbent is dimethyl 1,4-cyclohexyldicarb...

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Abstract

The invention relates to the field of production of ketene compounds, and discloses a method for preparing a ketene compound. The method comprises the following steps that (1) carrier gas, low carbonhydrocarbons, carboxylic acid and / or organic anhydride are preheated; (2) under the condition of high-temperature pyrolysis, the preheated materials in the step (1) are subjected to a high-temperaturepyrolysis reaction; (3) a high-temperature pyrolysis reaction product obtained in the step (2) is separated. According to the method, under the same production load, the yield of the ketene compoundis higher, there is less accumulated carbon in a reactor, in the same operation period, energy consumption of equipment is lower, and the production cost is lower.

Description

technical field [0001] The invention relates to the field of production of ketene compounds, in particular to a method for preparing ketene compounds. Background technique [0002] Ketone compound (RR'=C=O) is an important organic synthesis intermediate, its molecular structure has a high degree of unsaturation, and can undergo reactions such as addition, decomposition and polymerization. production material. For the preparation of enone compounds, researchers have proposed synthetic methods such as pyrolysis of fatty acids and fatty acid anhydrides, and dehalogenation of α-acyl halide compounds. Among them, the dehalogenation of α-acyl halide compounds has complicated steps and a large amount of solvent , many by-products and other issues. At present, high temperature pyrolysis of fatty acids or fatty acid anhydrides is often used in industry to prepare enone compounds [0003] U.S. Delware University discloses a kind of high specific surface area (>100m2) that is use...

Claims

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Application Information

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IPC IPC(8): C07C45/89C07C49/90C07C49/88
CPCC07C45/89C07C49/90C07C49/88
Inventor 时强王韩徐锦龙
Owner ZHEJIANG HENGYI PETROCHEMICAL RES INST CO LTD
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