CN1793124A - Process for refining high purifity hexanpropylamide - Google Patents
Process for refining high purifity hexanpropylamide Download PDFInfo
- Publication number
- CN1793124A CN1793124A CN 200510136647 CN200510136647A CN1793124A CN 1793124 A CN1793124 A CN 1793124A CN 200510136647 CN200510136647 CN 200510136647 CN 200510136647 A CN200510136647 A CN 200510136647A CN 1793124 A CN1793124 A CN 1793124A
- Authority
- CN
- China
- Prior art keywords
- organic solvent
- distillation
- hexanolactam
- extraction
- impurity
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Other In-Based Heterocyclic Compounds (AREA)
Abstract
The invention relates to a refine method for caprolactam that takes process of neutralization reaction, pre-refining, concentrating and distilling, and impurity extracting to caprolactam to gain high purity caprolactam. The invention is simple technology, sharply decreases power consumption and operating density. It improves the quality of the product, and declines cost.
Description
Technical field
The present invention relates to a kind of process for purification of hexanolactam.
Background technology
Hexanolactam, formal name used at school ε-Ji Neixianan, molecular formula C
6H
11NO, molecular weight are 113.16, structural formula:
Normal temperature is white crystal down, and fusing point is 69.3 ℃.As the monomer of polyamide 6, its a kind of important petrochemicals is widely used in making polyamide fibre and engineering plastics.
The preparation method of hexanolactam is more, has only several but quality can satisfy the commercial run of polymerization requirement and economical rationality." Organic Chemicals complete works " the 2nd edition the 3rd volume introduced caprolactam production method and industrial front, mainly contain pimelinketone-hydroxylamine assay, photo-nitrosation of cyclohexane process and toluene method etc., wherein preceding two class methods need prepare cyclohexanone-oxime by benzene, be rearranged into hexanolactam through Beckmann again, then a kind of method is raw material with toluene, produces hexahydrobenzoic acid and further nitrosification generation hexanolactam by oxidation, hydrogenation.Because the preparing process of caprolactam complexity, reaction process is numerous, no matter the crude caprolactam that adopts which kind of method to obtain all contains plurality of impurities.Though the total content of impurity is very little, bigger to the quality product influence, therefore suitable process for purification must be arranged as much as possible with its removal.
The preparation process of existing high purity caprolactam generally comprises refining three parts of reaction, pre-refining and distillation.Reactive moieties is converted into hexanolactam with raw material through chemical reaction, and makes crude caprolactam water solution; Crude caprolactam water solution partly is made into certain density smart caprolactam water solution by pre-refining; At last by concentrating the refining high purity caprolactam product that obtains.With nicotinic acid and cyclohexanone-oxime is that the reactive moieties of the hexanolactam preparation process of raw material mainly comprises and resetting and two reactions that neutralize; Pre-refining partly mainly includes machine solvent extraction, water back extraction and the such main procedure of hydrogenation, and such as the such supporting process of ion-exchange; Concentrated FF mainly comprises multiple-effect evaporation and multistage distillation process.This preparation process can guarantee that the steady quality of high purity caprolactam is reliable, but also has comparison significant disadvantages such as long flow path, investment is big, technology controlling and process is complicated, energy consumption is big.
The quality guarantee of high purity caprolactam depends primarily in the preparation process effective elimination to impurity.According to the difference of solubility property, the impurity in the crude caprolactam can be divided into inorganic and organic two big classes, and wherein organic impurity has two kinds of water-soluble and oil solubles again.Classify according to boiling point, organic impurity has two kinds: a kind of is the boiling point impurity lower than hexanolactam (abbreviation light impurity), as β hydroxy-cyclohexanone and other azanols etc., another kind is the boiling point impurity higher than hexanolactam (abbreviation heavy seeds), as organic hydrochlorate with at evaporation, the oligopolymer that generates in the still-process etc.Most of impurity among the existing preparation technology all partly is removed at pre-refining: discharge most inorganic impurity and water-soluble organic impurity with extracting phase (aqueous residue) in extraction process, in the back extraction process, take most oil soluble organic impurity out of subsequently with extracting phase (organic solvent phase), also can absorbed portion oil soluble organic impurity in this supporting process of follow-up ion-exchange.Remaining impurity is further removed at concentrated FF: the impurity that boiling point is lower turns back to the front operation with the multiple-effect evaporation water that contains a small amount of hexanolactam, to reduce the loss of hexanolactam; The higher impurity of boiling point is then stayed in the raffinate of multistage distillation, also is returned to the front operation, to reclaim hexanolactam.The extracting phase that comes out from the back extraction process is the organic solvent that contains certain impurity level, for the energy-conservation consideration that accumulates with the foreign matter content of controlling in the organic solvent, generally only the small part solvent is passed through to distill, and does not recycle by the distillatory solvent with major part.
Whether the finished product hexanolactam meets the requirements, and depends on the impurity equilibrium concentration under the stable state in the system to a great extent, and this numerical value is closely-related with organizing of the cutting ratio of the quality of Beckmann rearrangement reaction, vinasse and technical process.
Summary of the invention
The preparation method who the purpose of this invention is to provide the high purity caprolactam that a kind of flow process is short, investment is little, technology controlling and process is simple, energy consumption is little.
The objective of the invention is to realize in the following way: a kind of process for purification of high purity caprolactam:
1), using cyclohexanone-oxime Beckmann reset generated the hexanolactam sulfuric ester that contains impurity carry out neutralization reaction, in separator, isolate slightly oil of hexanolactam;
2), carry out pre-refining: pre-refining is stripped by organic solvent extraction, water and hydrogenation is formed, or organic solvent extraction, steam distillation and hydrogenation are formed.
3), to concentrate distillation refining, concentrates that distillation is refining to be made up of 2 and above distillation tower, first distillation tower is a pre-distillation column.
4), impurity extraction, forms by organic solvent extraction, water back extraction and organic solvent distillation, or organic solvent mixed dissolution, water back extraction and organic solvent distillation composition, obtain highly purified hexanolactam.
Neutralize with ammoniacal liquor.
Steam distillation can adopt the multi-effect distilling mode.
The organic solvent mixed dissolution is to be mixed and made into the solution that contains hexanolactam with organic solvent and from the hexanolactam vinasse that contains that distills refining system.
Organic solvent is alkane or the naphthenic hydrocarbon or the aromatic hydrocarbons of carbonatoms 4～8, or their mixture.
Organic solvent is benzene, toluene, hexanaphthene, normal hexane or its mixture.
Organic solvent after the impurity extraction all distills mutually, and the solvent cycle after the distillation is used.
Burning is directly sent in not recirculation of raffinate after the impurity extraction.
The present invention has following technique effect: (1) is compared with existing hexanolactam preparation method, increase impurity extracting and separating part, reducing the circulation of impurity in system, thereby the impurity equilibrium concentration under the stable state in can the reduction system makes the caprolactam product quality more controlled; (2) if adopt the combination of extraction and water vapor component distillation organic solvent to replace the combination of back extraction and multiple-effect evaporation, not only technology is simpler, and more energy-conservation.
Description of drawings
Fig. 1 is a process flow diagram of the present invention:
Embodiment
As shown in Figure 1, cyclohexanone-oxime and oleum enter reactive system A respectively, become crude caprolactam water solution about 70% through main procedures such as rearrangement, neutralization reactions; This aqueous solution enters the B of pre-refining system, through main procedures such as organic solvent extraction, steam distillation and hydrogenation, make 70%～90% smart caprolactam water solution, or, make 20%～40% smart caprolactam water solution through main procedures such as organic solvent extraction, steam distillation and hydrogenation; Enter and concentrate distillation refining system C,, or, obtain high-quality hexanolactam finished product or work in-process through main procedures such as multiple-effect evaporation and multistage distillations through main procedures such as fore-distillation and multistage distillations; From concentrating distillation refining system C isolated impure more hexanolactam (overhead product of fore-distillation and the raffinate of multistage distillation, or the part of multiple-effect evaporation steams the raffinate of thing and multistage distillation) be sent to the impurity extracting and separating D of system, become impure less caprolactam water solution after removing wherein most of impurity, sent back to reactive system A or the B of pre-refining system or reactive system A and the B of pre-refining system.
Embodiment:
The using cyclohexanone-oxime Beckmann rearrangement product contains about 51%, the free SO of hexanolactam about 43% (mass percent, down with), sulfuric acid
3About 4% and impurity 2%, its flow is 25.2m
3/ h enters mixing tank by pump, with 37.1m
3The flow of/h adds 20% ammoniacal liquor and neutralizes, in separator with 7.6m
3After/h circulation caprolactam water solution mixes, isolate slightly oil of hexanolactam, with 24.4m
3The flow of/h enters extraction tower.Cat head adds 54.4m
3The purified petroleum benzin of/h, extraction phase are used 0.8m again
3/ h water washs, and obtains benzene-caprolactam solution, contains wherein that hexanolactam is about 20.5%, benzene 76.8%, water 2.6% and impurity 0.1%.
The own solution of benzene is with 92.5m
3The flow of/h enters the triple effect distillation tower, and first column overhead distillates benzene 42.3m
3/ h, second column overhead distillates benzene 18.1m
3/ h is the own solution of benzene that contains hexanolactam 54.5% at the bottom of the tower, enters the 3rd tower.The 3rd tower steam rates is 0.24m
3/ h, normal pressure, temperature is 68.3 ℃ of distillations down, obtains 90% caprolactam water solution 18.6m at the bottom of the tower
3/ h enters hydrogenator.
Caprolactam solution behind the hydrogenation is heated to 126 ℃ with low-pressure steam, and steam separates with the own aqueous solution in vapour liquid separator, and the top is the hexanolactam water vapor that contains organic impurity, and the bottom is 99% caprolactam solution, and flow is about 17.0m
3/ h enters flash separator.The pressure of flash separator is about 9mmHg, and steam temperature is 200 ℃, and tolerance is 520m
3/ h.Top product is about 27% caprolactam water solution after condensation, and flow is about 4.8m
3/ h is sent to the impurity extraction tower.
Caprolactam concentration reaches 99.9% (about 16.1m behind the flash separator
3/ h), send into the hexanolactam distillation tower, cat head material refrigerated separation, pure hexanolactam is after quality inspection, with 15.3m
3The flow of/h enters the hexanolactam storage tank.Bottoms enters follow-up raffinate distillation and heavy residual distillation, and overhead condensate is all returned the hexanolactam distillation tower, and bottoms is with 0.7m
3The flow of/h enters the dissolving recovery system, with 3.2m
3/ h benzene mixes, isolate residue after, the hexanolactam benzole soln enters the impurity extraction tower.
It is 3.9m that the impure hexanolactam benzole soln of dissolving recovery system mixes the back total amount
3/ h, caprolactam concentration is 20.0%, enters the bottom of impurity extraction tower, by top-down water extraction recovery hexanolactam wherein, service temperature is 42 ℃.Water as extraction is made up of two portions, and first flash distillation water or fore-distillation water enter from back extraction tower middle part, and it two is a small amount of vaporize waters that enter from the back extraction top of tower.Extraction phase is that water (caprolactam water solution) goes out from tower bottom flow, and concentration is 24.1%, and flow is 4.7m
3/ h is with the water layer (1.1m after raffinate distillation phlegma, steam distillation cat head separate
3/ h) mix, sent to the preceding separator of hexanolactam extraction.The extracting phase that contains organic impurity is that benzene flows out from cat head, is sent to the benzene distillation tower then, and the effusive benzene vapour of benzene distillation column overhead is sent to the benzene groove and recycled after condensation, be the insoluble residue at the bottom of the tower, directly sends to and burns or comprehensive utilization.
Claims (8)
1, a kind of process for purification of high purity caprolactam is characterized in that:
1), using cyclohexanone-oxime Beckmann reset generated the hexanolactam sulfuric ester that contains impurity carry out neutralization reaction, in separator, isolate slightly oil of hexanolactam;
2), carry out pre-refining: pre-refining is stripped by organic solvent extraction, water and hydrogenation is formed, or organic solvent extraction, steam distillation and hydrogenation are formed.
3), to concentrate distillation refining: concentrate that distillation is refining to be made up of 2 and above distillation tower, first distillation tower is a pre-distillation column.
4), impurity extraction: forms by organic solvent extraction, water back extraction and organic solvent distillation, or organic solvent mixed dissolution, water back extraction and organic solvent distillation composition, obtain highly purified hexanolactam.
2, method according to claim 1 is characterized in that: the organic solvent mixed dissolution is to be mixed and made into the solution that contains hexanolactam with organic solvent and from the hexanolactam vinasse that contains that distills refining system.
3, method according to claim 1 is characterized in that: organic solvent is alkane or the naphthenic hydrocarbon or the aromatic hydrocarbons of carbonatoms 4～8, or their mixture.
4, method according to claim 3 is characterized in that: organic solvent is benzene, toluene, hexanaphthene, normal hexane or its mixture.
5, method according to claim 1 is characterized in that: the organic solvent after the impurity extraction all distills mutually, and the solvent cycle after the distillation is used.
6, method according to claim 1 is characterized in that: the not recirculation of raffinate after the impurity extraction, directly send into burning.
7, method according to claim 1 is characterized in that: steam distillation can adopt the multi-effect distilling mode.
8, method according to claim 1 is characterized in that: neutralize with ammoniacal liquor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101366478A CN100384818C (en) | 2005-12-27 | 2005-12-27 | Process for refining high purifity hexanpropylamide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101366478A CN100384818C (en) | 2005-12-27 | 2005-12-27 | Process for refining high purifity hexanpropylamide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1793124A true CN1793124A (en) | 2006-06-28 |
| CN100384818C CN100384818C (en) | 2008-04-30 |
Family
ID=36804786
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005101366478A Expired - Fee Related CN100384818C (en) | 2005-12-27 | 2005-12-27 | Process for refining high purifity hexanpropylamide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100384818C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102234248A (en) * | 2010-04-23 | 2011-11-09 | 中国石油化工股份有限公司 | Impurity extraction method for caprolactam production |
| CN103896838A (en) * | 2012-12-28 | 2014-07-02 | 帝斯曼知识产权资产管理有限公司 | Method and equipment for continuously producing epsilon-hexanolactam |
| CN104262252A (en) * | 2014-10-21 | 2015-01-07 | 湖南百利工程科技股份有限公司 | Method for separating caprolactam and sulphuric acids from caprolactam sulfate |
| CN104981454A (en) * | 2012-12-19 | 2015-10-14 | 巴斯夫欧洲公司 | Method for the production of purified caprolactam from the beckmann rearrangement of cyclohexanone oxime |
| CN107556240A (en) * | 2016-08-24 | 2018-01-09 | 沧州旭阳化工有限公司 | A kind of system of caprolactam refining method and refined caprolactam |
| CN110804018A (en) * | 2019-12-11 | 2020-02-18 | 河北美邦工程科技股份有限公司 | Refining method and refining system of caprolactam |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| PL206266B1 (en) * | 2001-03-01 | 2010-07-30 | Dsm Ip Assets Bvdsm Ip Assets Bv | Process for recovering and purifying caprolactam from an organic solvent |
| CN1259310C (en) * | 2004-09-24 | 2006-06-14 | 中国石油化工股份有限公司 | Process for extracting and separating caprolactam from amide oil |
-
2005
- 2005-12-27 CN CNB2005101366478A patent/CN100384818C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102234248A (en) * | 2010-04-23 | 2011-11-09 | 中国石油化工股份有限公司 | Impurity extraction method for caprolactam production |
| CN104981454A (en) * | 2012-12-19 | 2015-10-14 | 巴斯夫欧洲公司 | Method for the production of purified caprolactam from the beckmann rearrangement of cyclohexanone oxime |
| CN104981454B (en) * | 2012-12-19 | 2017-10-24 | 巴斯夫欧洲公司 | The method that the caprolactam of purifying is prepared by the Beckmann rearrangement of cyclohexanone oxime |
| CN103896838A (en) * | 2012-12-28 | 2014-07-02 | 帝斯曼知识产权资产管理有限公司 | Method and equipment for continuously producing epsilon-hexanolactam |
| CN103896838B (en) * | 2012-12-28 | 2018-03-23 | Cap Iii 有限公司 | The method and apparatus of continuous production ε caprolactams |
| CN104262252A (en) * | 2014-10-21 | 2015-01-07 | 湖南百利工程科技股份有限公司 | Method for separating caprolactam and sulphuric acids from caprolactam sulfate |
| CN107556240A (en) * | 2016-08-24 | 2018-01-09 | 沧州旭阳化工有限公司 | A kind of system of caprolactam refining method and refined caprolactam |
| CN107556240B (en) * | 2016-08-24 | 2020-10-30 | 沧州旭阳化工有限公司 | Caprolactam refining method and system |
| CN110804018A (en) * | 2019-12-11 | 2020-02-18 | 河北美邦工程科技股份有限公司 | Refining method and refining system of caprolactam |
| CN110804018B (en) * | 2019-12-11 | 2023-10-31 | 河北美邦工程科技股份有限公司 | Refining method and refining system of caprolactam |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100384818C (en) | 2008-04-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8492586B2 (en) | Process for preparation of formate salt | |
| CN100384818C (en) | Process for refining high purifity hexanpropylamide | |
| US5028735A (en) | Purification and preparation processes for methyl methacrylate | |
| US9073847B2 (en) | Method and an arrangement for separating at least one carboxylic acid and furfural from a dilute aqueous mixture thereof | |
| TW200800806A (en) | Method of recovering triethylamine in water | |
| CN104926690B (en) | The recovery process for purification and device of acetonitrile in a kind of synthesis for Ceftriaxone Sodium | |
| CN102875468A (en) | Method for producing caprolactam through gas phase rearrangement of cyclohexanone-oxime | |
| CN105837394A (en) | Purifying method of highly-pure 1,2,3-trimethylbenzene | |
| CN105793220A (en) | Process for removal of sulphur from raw methanol | |
| EP1289948B1 (en) | Method for purifying lactams | |
| CN101255122A (en) | Method for purifying dimethylacetamide from spinning wastewater | |
| CN114436883B (en) | Method for recovering N, N-dimethylacetamide from multi-element solution system | |
| CN106349107A (en) | Method and device for separating acetonitrile-triethylamine mixture through heterogeneous azeotropic rectification | |
| US11142510B2 (en) | System and method for continuously preparing furfural using acid-containing pentose solution | |
| JPS6025949A (en) | High boiling point solvents for recovering acetic acid from aqueous solution | |
| CN109679679A (en) | A kind of heavy aromatics industrial process | |
| US8084651B2 (en) | Process for purification of glycerol | |
| CN111100055A (en) | Extraction-rectification recovery method of N-methyl pyrrolidone in waste solvent | |
| CN101092389A (en) | Method for preparing high-purity anthracene and carbazole by rectifying crude anthracene | |
| US2012125A (en) | Water soluble resinate production | |
| US1997171A (en) | Production of pure by-products from resin-containing liquors | |
| CN111471015B (en) | Device and method for recycling caprolactam in benzene distillation residual liquid | |
| CN116023660A (en) | Solvent recovery method and system in polyphenylene sulfide production process and related application | |
| CN103896841B (en) | The method for being recycled from organic solvent and purifying epsilon-caprolactams | |
| CN117946005A (en) | Method for refining and purifying caprolactam distillation heavy residual liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: CHINA PETROCHEMICAL CO., LTD. Effective date: 20120510 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20120510 Address after: 411105 Hunan city of Xiangtan province donkey Tang Xiangtan University Co-patentee after: Sinopec Corp. Patentee after: Xiangtan University Address before: 411105 Hunan city of Xiangtan province donkey Tang Xiangtan University Patentee before: Xiangtan University |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080430 Termination date: 20121227 |