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Low-cost separation method and device for fatty acid mixture

A technology of mixed fatty acid and separation method, applied in the field of low-cost separation method and separation device of mixed fatty acid, can solve the problems of difficult separation of high value-added products, low product yield and purity, and excessive heat-sensitive decomposition, etc. Condensation, good product quality, good heat transfer effect

Inactive Publication Date: 2016-07-06
张志炳
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] For the mixed fatty acid system containing saturated fatty acids, monounsaturated fatty acids and polyunsaturated fatty acids, the existing separation and refining processes generally have small scale, high energy consumption, low product yield and purity, more thermal decomposition and high added value. Product separation is difficult and many other defects

Method used

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  • Low-cost separation method and device for fatty acid mixture

Examples

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Embodiment 1

[0018] Example 1: A 5kt / aC12~C22 fatty acid continuous refining project

[0019] The continuous refining process of fatty acids such as figure 1 shown. The component mass fractions of fatty acid raw materials are as follows: C12-C14: 5%-15%; C16: 20%-30%; C18: 55%-65%; C22: 1%-3%, and the heavy component is less than 1%. The processing capacity is 625kg / h. The diameter of the vacuum rectification tower T1 is 1400mm, the total height is 32000mm, and its distillation section is provided with 16000mm SINOPAK-B2 wallless flow structured wire mesh filler, which is divided into 3 sections. The liquid distribution adopts LQ-II infinite point liquid distributor, and the top reflux part adopts spray equipment. The stripping section is equipped with 18 STV super valve trays. The tower kettle of the rectification tower is funnel-shaped, wherein the diameter of the thin tube part is 250mm, the height of the thin tube part is 2800mm, and the height of the necking part at the upper part...

Embodiment 2

[0022] Example 2: A 10kt / aC12~C22 fatty acid continuous refining project

[0023] The continuous refining process of fatty acids such as figure 1 shown. The component mass fractions of fatty acid raw materials are as follows: C12~C14: 4%~10%; C16: 25%~30%; C18: 55%~60%; C22: 1%~2%, and the heavy component is less than 1%. The amount is 1250kg / h. The vacuum rectification tower T1 has a diameter of 2000mm and a total height of 36000mm, and its rectification section is equipped with a regular wire mesh packing of 18000mm, which is divided into 3 sections. The top reflux part adopts spray equipment, and the liquid distribution adopts infinite point liquid distributor. The stripping section is equipped with a regular wire mesh packing of 16000 mm, and the bottom of the rectification tower is funnel-shaped, in which the diameter of the thin tube part is 500 mm, the height of the thin tube part is 3000 mm, and the height of the narrow part of the upper part of the funnel is 600 mm. ...

Embodiment 3

[0025] According to measurement and calculation, compared with the existing technology for separating mixed fatty acids by using this method and device, the yield can be increased by 6.6%, the energy consumption per unit product can be saved by 40.6%, and the investment in raw material equipment per ton can be saved by more than 42%. Example 3: A 100kt / aC12~C22 fatty acid continuous refining project

[0026] The continuous refining process of fatty acids such as figure 1 shown. The component mass fractions of fatty acid raw materials are as follows: C12~C14: 5%~10%; C16: 23%~35%; C18: 50%~68%; C22: 2%~3%, the heavy component is less than 1%. The amount is 12500kg / h,

[0027] The rectification tower T1 has a diameter of 6000mm and a total height of 40000mm. The rectification section is set at 20000mm, and the structured wire mesh packing is divided into 3 sections. Liquid distribution uses an infinite point liquid distributor. The stripping section is equipped with 24 STV s...

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Abstract

The invention discloses a low-cost separation method and device for fatty acid mixture.A decompression rectifying tower is used for continuously separating and refining C12-C22 fatty acid components.A direct contact condensation mode is adopted in the tower top to efficiently cool rising material steam, the cooled rising material steam is processed by a heat recovery boiler into secondary steam to be used, a vapor-phase product on the tower bottom is processed by a demister and then condensed, and acceptable products are extracted.Residues on the tower bottom enter a wiped film evaporator and an erucic acid refining tower to be separated, and high-purity erucic acid is acquired.In the whole process, by means of thermal coupling gradient utilization, the heat consumption in the production process is minimized, and low cost, low emission and high yield are achieved.

Description

technical field [0001] The invention relates to the field of chemical industry, in particular to a low-cost separation method of mixed fatty acids and a separation device thereof. Background technique [0002] Fatty acids are a class of carboxylic acid compounds composed of hydrocarbon groups linked to carboxyl groups. They are important industrial raw materials and basic raw materials for oleochemicals. According to the length of the carbon chain, fatty acids can be divided into short-chain fatty acids with less than 6 carbon atoms in the carbon chain; medium-chain fatty acids with 6-12 carbon atoms in the carbon chain, mainly caprylic acid and capric acid; long-chain fatty acids Fatty acid, the number of carbon atoms in its carbon chain is greater than 12. Can also be divided into three classes according to whether the carbon-hydrogen bond on its carbon-hydrogen main chain is saturated or not: saturated fatty acid, the carbon-hydrogen bond on its carbon-hydrogen main chai...

Claims

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Application Information

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IPC IPC(8): C11C1/10B01D3/14B01D3/10B01D3/26C07C51/43C07C51/44C07C57/03
CPCB01D3/10B01D3/148B01D3/26C07C51/43C07C51/44C11C1/10C07C57/03Y02P20/10Y02P70/10
Inventor 张志炳张锋王宝荣邓自磊
Owner 张志炳
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