CN111004130B - Method for purifying 1,2-propane diamine - Google Patents
Method for purifying 1,2-propane diamine Download PDFInfo
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- CN111004130B CN111004130B CN201911315323.9A CN201911315323A CN111004130B CN 111004130 B CN111004130 B CN 111004130B CN 201911315323 A CN201911315323 A CN 201911315323A CN 111004130 B CN111004130 B CN 111004130B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/82—Purification; Separation; Stabilisation; Use of additives
- C07C209/84—Purification
Abstract
The invention disclosesA method for purifying 1,2-propane diamine is provided, and C is adopted 2 ‑C 3 One or C of dihydric alcohol(s) 2 ‑C 3 The composite extractant consists of alcohol amine and sodium tribromoacetate or tricresyl phosphate. Pumping the compound extractant and 1,2-propane diamine crude product into an extraction tower by using an extractant feed pump and a crude product feed pump, and extracting 1,2-propane diamine from the tower top of the extraction tower; pumping the tower bottom material of the extraction tower into the rectification tower by using an extraction tower bottom pump, circulating the extractant in the rectification tower back to the extraction tower by using an extractant circulating pump, and extracting water from the top of the rectification tower. After the composite extractant is used, the tower height and the reflux ratio are reduced, the separation efficiency is improved, the extractant can be repeatedly used after being simply separated, the energy consumption is greatly reduced, and the production cost is reduced. Has the advantages of high separation efficiency, high purity of purified products, good product chromaticity and recyclable extracting agent.
Description
Technical Field
The invention belongs to the technical field of fine chemical separation and purification, and particularly relates to a method for purifying 1,2-propane diamine.
Background
1,2-propanediamine, also known as 1,2-diaminopropane, formula C 3 H 10 N 2 1,2-propane diamine is an organic chemical and fine chemical with wide development prospect. Is mainly used for producing mineral dressing medicament,The metal passivator, the aviation resin curing agent and the rubber vulcanization accelerator are also used for dyes, electroplating and analytical reagents, are also important fine chemical intermediates, and have wide application in the fields of organic synthesis, medicines, dyes, pesticides, chemical auxiliaries, rubber plastic auxiliaries, epoxy resin curing agents and the like.
Isopropanolamine is selected as a raw material, and 1,2-propane diamine can be prepared in high selectivity by hydrogenation, reduction and amination, and the environment friendliness of the process is more and more emphasized. However, in the process of preparing 1,2-propanediamine by using isopropanolamine, water is generated by the reaction. Because the boiling point of 1,2-propane diamine is 118.9 ℃, the boiling point of water is 100 ℃, the two have near azeotropic phenomenon, and when the purity of 1,2-propane diamine is more than 98%, the relative volatility of the two is less than 1.02, and the separation difficulty is large. In order to obtain a product with the water content of less than 1.0 percent, the theoretical plate number is more than 80, the reflux ratio is more than 30, the equipment investment is large, the energy consumption is huge, and simultaneously, as 1,2-propane diamine is taken out from a tower kettle, the color turns yellow, the product chroma is more than 50 Hazen, the requirements of application fields such as medicines cannot be met, and the industrial preparation of 1,2-propane diamine is influenced.
Disclosure of Invention
In view of the defects or shortcomings in the technology, the invention aims to provide a method for purifying 1,2-propane diamine, which has the advantages of low equipment investment, low energy consumption and high product quality.
The invention provides a method for purifying 1,2-propane diamine, which comprises the following steps:
(1) Pumping the compound extractant and 1,2-crude propane diamine into an extraction tower by using an extractant feed pump and a crude product feed pump, wherein the number of theoretical plates of the extraction tower is not more than 15,1,2-crude propane diamine feed position is 10-13 theoretical plates; the feeding position of the extractant is 3 to 5 theoretical plates, the mass ratio of 1,2-propane diamine crude product to the extractant is 1.5 to 0.8, the reflux ratio is 0.2 to 5:1, 1,2-propane diamine is extracted from the top of the extraction tower, the purity is more than 99.999 percent, and the water content is less than 10ppm;
(2) Pumping the tower bottom material of the extraction tower into a rectifying tower by using an extraction tower bottom pump, wherein the number of theoretical plates of the rectifying tower is not more than 10, the feeding position is 5-7 theoretical plates, the reflux ratio is 1:1-5, an extracting agent in the rectifying tower circulates back to the extraction tower through an extracting agent circulating pump, and water is extracted from the top of the rectifying tower.
The main component of the composite extractant is C 2 -C 3 One or C of dihydric alcohol(s) 2 -C 3 The residual component of the alcohol amine is sodium tribromoacetate or tricresyl phosphate.
The sodium tribromoacetate in the composite extracting agent accounts for 0.5% of the total mass of the composite extracting agent.
In the composite extracting agent, tricresyl phosphate accounts for 0.3% of the total mass of the composite extracting agent.
The method for purifying 1,2-propane diamine uses the composite extracting agent, reduces the tower height and reflux ratio, improves the separation efficiency, can be repeatedly used after the composite extracting agent is simply separated, greatly reduces the energy consumption and reduces the production cost; meanwhile, 1,2-propane diamine is directly extracted from the top of the extraction tower, so that the product does not have the phenomenon of decomposition caused by heating product flow in the tower kettle in the traditional process, the phenomenon of accumulation of decomposition products in a system does not exist, the problem that the product chromaticity meets the requirement does not exist, and the product chromaticity is less than 10 Hazen. The method has the advantages of high separation efficiency, high purity of purified products, good product chromaticity and recyclable extracting agent.
Drawings
FIG. 1 is a schematic diagram of an apparatus and process for purifying 1,2-propanediamine according to the present invention. The symbols in the figures represent:
b1, an extractant feeding pump, B2, a crude product feeding pump, B3 and an extraction tower; b4, a rectifying tower; b5, an extraction tower bottom pump, B6 and an extractant circulating pump
1. Enter extractant charge pump B1,2, enter crude charge pump B2,3, enter extraction column B3 through extractant charge pump B1, 4, enter extraction column B3 through crude charge pump B2, 5, flow out from extraction column B3, 6, flow out from extraction column B3 and enter extraction column kettle bottom pump B5,7, flow out from extraction column kettle bottom pump B5 and enter rectifying column B4,8, flow out from rectifying column B4, 9, flow out from rectifying column B4 and enter extractant circulating pump B6,10, flow to extraction column B3 from extractant circulating pump B6.
Detailed Description
The present invention will be described in further detail with reference to the following drawings and examples.
As shown in FIG. 1, the method for purifying 1,2-propanediamine as given in the following example uses equipment comprising extractant feed pump B1, crude product feed pump B2, extraction column B3, rectification column B4, extraction column bottom pump B5 and extractant circulation pump B6; an extractant feed pump B1 and a crude product feed pump B2 are connected with an extraction tower B3, 1,2-propanediamine is extracted from the top of the extraction tower B3, the extraction tower B3 is connected with a rectification tower B4 through an extraction tower bottom pump B5, water is extracted from the top of the rectification tower B4, and the rectification tower B4 is connected with the extraction tower B3 through an extractant circulating pump B6.
The purity of the purified 1,2-propane diamine is detected by gas chromatography, the chromatographic conditions are that a gasification chamber is 250 ℃, a detector is 250 ℃, a chromatographic column is a CAM column, the specifications are 30m multiplied by 0.32mm multiplied by 0.25um, and the column temperature is 70 ℃.
The water content of the purified 1,2-propanediamine was measured using karl Fei Xiufa and the chroma was determined using CS-810 transmission spectrocolorimeter.
The following are examples given by the inventors, and the present invention is not limited to these examples.
Example 1:
respectively pumping an extractant and 1,2-crude propylenediamine into an extraction tower B3 by using an extractant feeding pump B1 and a crude product feeding pump B2, wherein the number of theoretical plates of the extraction tower B3 is 15,1,2-crude propylenediamine feeding positions are 10 theoretical plates, the main component of the composite extractant is ethylene glycol, the rest components are 0.5 percent of sodium tribromoacetate, the composite extractant feeding position is a 3 rd theoretical plate, the mass ratio of 1,2-crude propylenediamine to the composite extractant is 1.5, the reflux ratio is 5:1, and 1,2-propylenediamine is extracted from the top of the extraction tower B3; the tower bottom material of the extraction tower B3 is pumped into a rectification tower B4 by an extraction tower bottom pump B5, the number of theoretical plates of the rectification tower B4 is 10, the feeding position is on the 5 th theoretical plate, the reflux ratio is 1:1, the tower top produced water of the rectification tower B4, the extracting agent in the rectification tower B4 is circulated back to the extraction tower B3 for reuse by an extracting agent circulating pump B6, the purity of 1,2-propane diamine is 99.99 percent by gas chromatography detection, colorless transparent liquid (chroma 6 Blacken), and the water content is 100ppm.
Example 2:
the same operation as in example 1, except that the theoretical plate number of the extraction column B3 is 15,1,2-crude propylenediamine is fed at 13 theoretical plates, the main component of the composite extractant is isopropanolamine, the remaining component is 0.3% tricresyl phosphate, the extractant is fed at 5 theoretical plates, the mass ratio of 1,2-crude propylenediamine to the composite extractant is 1.6, and the reflux ratio is 3:1; the number of theoretical plates of the rectifying tower B4 is 10, the feeding position is on the 6 th theoretical plate, the reflux ratio is 1:3, the purity of 1,2-propanediamine is 99.999 percent through gas chromatography detection, colorless transparent liquid (chroma is 4 Blacker), and the water content is 8ppm.
Example 3:
the same operation as in example 1, except that the number of theoretical plates of the extraction column B3 is 15,1,2-crude propylenediamine is at 11 theoretical plates, the main component of the composite extractant is 1,2-propanediol, the remaining component is 0.5% sodium tribromoacetate, the feeding position of the composite extractant is at 4 th theoretical plate, the mass ratio of 1,2-crude propylenediamine to composite extractant is 1.8, and the reflux ratio is 0.2; the number of theoretical plates of the rectifying tower B4 is 10, the feeding position is on the 7 th theoretical plate, the reflux ratio is 1:5, the purity of 1,2-propane diamine is 99.99 percent through gas chromatography detection, colorless transparent liquid (chroma is 9 Heiyang), and the water content is 95ppm.
Example 4:
the same operation as in example 1, except that the number of theoretical plates of the extraction column B3 was 15,1,2-crude propylenediamine feed position was 12 theoretical plates, the main component of the composite extractant was ethanolamine, the remaining component was 0.5% sodium tribromoacetate, the feed position of the composite extractant was 5 theoretical plates, the mass ratio of 1,2-crude propylenediamine to the composite extractant was 1.8, and the reflux ratio was 0.8; the number of theoretical plates of the rectifying tower B4 is 10, the feeding position is on the 6 th theoretical plate, the reflux ratio is 1:3, the purity of 1,2-propanediamine is 99.99 percent by gas chromatography detection, colorless transparent liquid (chroma is 8 Blacker) and the water content is 85ppm.
Example 5:
the same operation as in example 1, except that the number of theoretical plates of the extraction column B3 was 15,1,2-crude propylenediamine feed position was 10 theoretical plates, the main component of the composite extractant was 1,3-propanediol, the remaining component was 0.5% sodium tribromoacetate, the extractant feed position was 3 theoretical plates, the mass ratio of 1,2-crude propylenediamine to composite extractant was 1.6, and the reflux ratio was 1:1; the number of theoretical plates of the rectifying tower B4 is 10, the feeding position is on the 7 th theoretical plate, the reflux ratio is 1:2, the purity of 1,2-propanediamine is 99.999 percent through gas chromatography detection, colorless transparent liquid (chroma is 5 Blacker), and the water content is 7ppm.
Comparative example 1:
the same operation as in example 1, except that the number of theoretical plates of the extraction column B3 was 20,1,2-crude propylenediamine feed position was 14 theoretical plates, the extractant was ethylene glycol, the extractant feed position was 3 theoretical plates, the weight ratio of 1,2-crude propylenediamine to the extractant was 1.5, the reflux ratio was 5:1; the number of theoretical plates of the rectifying tower B4 is 15, the feeding position is on the 8 th theoretical plate, the reflux ratio is 1:1, the purity of 1,2-propane diamine is 99.85 percent (chroma is 56 Blacker) through gas chromatography detection, and water is not detected.
Comparative example 1:
the same operation as in example 1, except that the number of theoretical plates of the extraction column B3 was 20,1,2-crude propylenediamine feed position was 14 theoretical plates, the extractant was isopropanolamine, the extractant feed position was 3 theoretical plates, the weight ratio of 1,2-crude propylenediamine to the extractant was 1.5, the reflux ratio was 5:1; the number of theoretical plates of the rectifying tower B4 is 15, the feeding position is on the 8 th theoretical plate, the reflux ratio is 1:1, the purity of 1,2-propane diamine is 99.85 percent (chroma is 51 Blacker) through gas chromatography detection, and water is not detected.
Comparative example 3:
the crude product is directly rectified on a rectifying column with the theoretical plate number of 85, the reflux ratio is 30.
Claims (1)
1. A method of purifying 1,2-propanediamine comprising the steps of:
(1) By C 2 -C 3 One or C of dihydric alcohol(s) 2 -C 3 A composite extractant consisting of alcohol amine and sodium tribromoacetate accounting for 0.5 percent of the mass of the composite extractant, or C 2 -C 3 One or C of dihydric alcohol(s) 2 -C 3 The composite extractant composed of the alcohol amine and tricresyl phosphate accounting for 0.3 percent of the mass of the composite extractant is pumped into an extraction tower together with 1,2-crude propane diamine by an extractant feeding pump and a crude product feeding pump, and the feeding position of the extraction tower theoretical plate number is not more than 15,1,2-crude propane diamine is 10-13 theoretical plates; the feeding position of the extractant is 3 to 5 theoretical plates, the mass ratio of 1,2-propane diamine crude product to the extractant is 1.5 to 0.8, the reflux ratio is 0.2 to 5:1, 1,2-propane diamine is extracted from the top of the extraction tower, the purity is more than 99.999 percent, and the water content is less than 10ppm;
(2) Pumping the tower bottom material of the extraction tower into a rectifying tower by using an extraction tower bottom pump, wherein the number of theoretical plates of the rectifying tower is not more than 10, the feeding position is 5-7 theoretical plates, the reflux ratio is 1:1-5, an extracting agent in the rectifying tower circulates back to the extraction tower through an extracting agent circulating pump, and water is extracted from the top of the rectifying tower.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103073433A (en) * | 2012-12-17 | 2013-05-01 | 浙江赞宇科技股份有限公司 | Energy-saving recovery technology of 3-dimethylaminopropylamine (DMAPA) |
| CN103319350A (en) * | 2013-05-14 | 2013-09-25 | 西安近代化学研究所 | Purification method of 1,2-propylene amide |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103073433A (en) * | 2012-12-17 | 2013-05-01 | 浙江赞宇科技股份有限公司 | Energy-saving recovery technology of 3-dimethylaminopropylamine (DMAPA) |
| CN103319350A (en) * | 2013-05-14 | 2013-09-25 | 西安近代化学研究所 | Purification method of 1,2-propylene amide |
Non-Patent Citations (1)
| Title |
|---|
| 二氯丙烷氨化合成丙二胺工艺及动力学研究;谢永居;《浙江大学硕士学位论文》;20081231;全文 * |
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