CN1778795A - Production of hexyl lactam - Google Patents
Production of hexyl lactam Download PDFInfo
- Publication number
- CN1778795A CN1778795A CN 200410088696 CN200410088696A CN1778795A CN 1778795 A CN1778795 A CN 1778795A CN 200410088696 CN200410088696 CN 200410088696 CN 200410088696 A CN200410088696 A CN 200410088696A CN 1778795 A CN1778795 A CN 1778795A
- Authority
- CN
- China
- Prior art keywords
- diacetyl oxide
- hexanolactam
- solution
- acetate
- oxime
- 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
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Production of caprolactam is carried out by mixing organic solvent with acetic anhydride to obtain homogeneous phase acetic anhydride solution, adding cyclohexanone-oxime or its solution into acetic anhydride solution, homogeneous rearrangement reacting at rearrangement temperature, extracting liquid phase after rearrangement reacting by water, obtaining aqueous phase containing caprolactam, acetic anhydride and acetic acid, treating by organic solvent, circulation using, extracting aqueous phase by extracting agent, separating for caprolactam, acetic anhydride and acetic acid, entering caprolactam into refining part, converting acetic anhydride and acetic acid into acetic anhydride and circulation using. It has high conversion rate and selectivity, no by products and circulating use.
Description
Technical field
The invention relates to a kind of method for preparing hexanolactam.Specifically, be about a kind of in homogeneous system cyclohexanone-oxime generation Beckmann rearrangement prepare the method for hexanolactam.
Background technology
Hexanolactam is a kind of important Organic Chemicals of extensive application, and about in the world 90% hexanolactam is prepared by Beckmann rearrangement by cyclohexanone-oxime.Traditional Beckmann rearrangement process is: adopt oleum to make cyclohexanone-oxime form vitriolic hexanolactam salt, and for the high yield that obtains hexanolactam need add excessive sulfuric acid, use the ammoniacal liquor neutralise mixt then, obtain sulphur ammonium and hexanolactam.In typical industrial rearrangement process, the transformation efficiency of cyclohexanone-oxime is almost 100%, is 99% to the selectivity of hexanolactam, but every kilogram of oxime or every 1.0-1.3mol oxime will produce 1.3-1.8 kilogram sulphur ammonium simultaneously.This traditional technology uses oleum to be catalyzer and solvent, meeting severe corrosion equipment, harm environment, and consume the sulfuric acid and the ammonia of high value, the sulphur ammonium of a large amount of low values of by-product has increased production cost.Therefore the Beckmann rearrangement novel process of the no sulphur ammonium by-product of exploitation meets the Green Chemistry developing direction, is the improved target of preparing process of caprolactam.
From later 1960s, people just begin one's study and do not use the improved rearrangement technology of oleum, comprise vapor phase rearrangement technology and liquid phase rearrangement technology.In recent years, SUMITOMO CHEMICAL company is obtaining bigger progress aspect the vapor phase rearrangement research, but vapor phase rearrangement technology is unsuitable for existing installation is carried out technological transformation; Liquid phase rearrangement technology has the reaction conditions gentleness, to equipment requirements advantages of higher not, come into one's own all the time, and obtain some achievements in research.
Disclosed a kind of ammoniacal liquor neutral of avoiding among the GB1029201 and reset technology: in the catalyst system that anhydrous acetic acid, diacetyl oxide and sulfonic acid type ion exchange resin are formed, cyclohexanone-oxime generation rearrangement reaction, suitable temperature of reaction is 107-120 ℃, the hexanolactam that generates combines with the sulfo group of ion exchange resin, then ion exchange resin is separated from the rearrangement system, obtain hexanolactam with the water treatment ion exchange resin that is lower than 5 ℃ again, the productive rate of hexanolactam reaches 95.5%.
US5, with alkylating reagent and N, when dinethylformamide was made the liquid phase rearrangement catalyst system of solvent composition cyclohexanone-oxime, the transformation efficiency of cyclohexanone-oxime was 100%, the selectivity of hexanolactam is 99.8% in 225,547.
Open among flat 9-227509 and the flat 9-227510 of Te Kai the spy and to adopt N, dinethylformamide is solvent, when forming catalyst system with HCl and hydroxyl phosphorus trichloride, and the transformation efficiency of cyclohexanone-oxime can reach 100%, the selectivity and the yield of hexanolactam can reach 95%.
At US5,571,913 and EP0,639, the Zeo-karb that uses the sulfo group benzene ring structure among the 565A1 uses hexanoyl imido grpup-O-sulfonic acid to make cocatalyst as the rearrangement of cyclohexanone-oxime catalysts, the hexanolactam yield is 100%, and the amount of vitriol by product is lower than 5%.
Though the selectivity of the transformation efficiency of cyclohexanone-oxime and hexanolactam is higher in the above-mentioned patent, owing to economically with technologic reason, the catalytic liquid phase rearrangement technology of non-oleum fails to realize industrialization so far.
At present, developing the subject matter that the liquid phase Beckmann rearrangement technology of no sulphur ammonium by-product faces is: (1) is to use ion exchange resin fractionation by adsorption hexanolactam though reset no sulphur ammonium by-product in the technology at diacetyl oxide and acetic acid catalysis, and treatment capacity is less; (2) though at N, the hexanolactam yield of rearrangement reaction is very high in dinethylformamide, the methyl-sulphoxide equal solvent, but above-mentioned solvent and most solvent have good mutual solubility property, therefore are difficult to realize separating of catalyzer and rearrangement reaction product by methods such as solvent extractions; (3) after rearrangement reaction finishes, the processing step that adds excessive ammonia to system is infeasible, meeting by-product sulphur ammonium or other ammonium salt, and cause catalyzer not recycle; (4) some catalyzer is (as POCl
3, PCl
5And SO
3Deng) can harm physical environment and health of human body.
Summary of the invention
The objective of the invention is does not have the problems referred to above that sulphur ammonium by-product liquid phase rearrangement technology faces at present exploitation, propose a kind of in homogeneous system, the Beckmann rearrangement of catalysis of pimelinketone oxime prepares the novel process of hexanolactam, and reaching by solvent extraction and separation catalyzer and hexanolactam, realization does not have the purpose that sulphur ammonium by-product and catalyzer and organic solvent recycle.
Method provided by the invention is: with organic solvent and the mixed homogeneous phase solution of acetic anhydride that gets of diacetyl oxide; Under the rearrangement reaction temperature, will carry out the homogeneous phase rearrangement reaction in cyclohexanone-oxime or its solution adding solution of acetic anhydride; Liquid phase after the water extraction rearrangement reaction, acquisition contains the water of hexanolactam, diacetyl oxide and acetate, and organic solvent recycles after handling; Use the extraction agent aqueous phase extracted, the realization hexanolactam separates with diacetyl oxide and acetate; Hexanolactam enters refined unit; Diacetyl oxide and acetate recycle after changing into diacetyl oxide.
Use diacetyl oxide to be catalyzer in the inventive method, the part diacetyl oxide is converted into acetate in the rearrangement reaction process.
Said organic solvent should dissolve each other fully with diacetyl oxide in the inventive method, the existence of organic solvent not only can make reacting balance carry out, but also can reduce interaction between hexanolactam and diacetyl oxide, the acetate, help realizing that by method of extraction diacetyl oxide, acetate separate with hexanolactam.
The suitable organic solvent that is adopted among the present invention is most of common organic solvents, comprise: benzene,toluene,xylene, trimethylbenzene, propyl carbinol, hexanol, octanol, ether, n-butyl ether, ethyl acetate, butylacetate, pentyl acetate, methylene dichloride, trichloromethane, tetracol phenixin, 1,2-ethylene dichloride, chlorobutane and comprise the organic carboxyl acid of acetate, propionic acid, butyric acid, caproic acid.
In the homogeneous catalysis system solution of organic solvent and diacetyl oxide composition, the volumetric concentration of diacetyl oxide is 1.0%-80%, and preferred volume concentration is 10%-30%.
The Beckmann rearrangement temperature that is adopted in the inventive method is the boiling point of room temperature to organic solvent, preferred 40-80 ℃.
The cyclohexanone-oxime that adds catalyst system in the inventive method is the liquid or solid-state pure cyclohexanone-oxime that is below or above the rearrangement reaction system temperature, or is dissolved in the cyclohexanone-oxime solution in the organic solvent.The organic solvent that is used to dissolve cyclohexanone-oxime can be identical with the organic solvent of forming homogeneous catalysis system, also can be different.As use cyclohexanone-oxime solution, then its suitable concentration is 0.2-4.0mol/L, preferred 1.5-2.5mol/L.
The mol ratio of cyclohexanone-oxime and diacetyl oxide consumption is 1 in the inventive method: (1.0-3.0), and preferred 1: (1.3-2.0).
Adopting the purpose of water extraction organic solution in the inventive method is that hexanolactam, diacetyl oxide and acetate are all transferred to water, and above-mentioned several materials are easier to be dissolved in the water, can make these several materials transfer to water fully by the extraction of 3-4 level.The purified processing of extracting phase organic solvent can be further used for preparing solution of acetic anhydride, thereby realizes recycling of organic solvent.Under comparatively high temps, the diacetyl oxide in the aqueous solution could be converted into acetate fully, therefore still has diacetyl oxide in the aqueous solution.
The extraction agent that is used for aqueous phase extracted in the inventive method can be neutral phosphorus-based extractant or saturated hydrochloric ether.
In the inventive method as extraction agent neutral phosphorus-based extractant comprise tributyl phosphate (TBP), trioctyl phosphate, tricresyl phosphate alkane ester, TRPO (TRPO) etc., can directly use above-mentioned neutral phosphorus-based extractant, or they are dissolved in the organic solvent as extraction agent.The two-phase system that extraction agent and water are formed is realized separating of hexanolactam and diacetyl oxide, acetate by complexing solvent extraction principle.The organic solvent of dissolving neutral phosphorus-based extractant mainly is alkane and aromatic hydrocarbons, and as normal hexane, normal heptane, octane-iso, sherwood oil, benzene,toluene,xylene etc., the volumetric concentration of neutral phosphorus-based extractant is 10%-95%.
Saturated hydrochloric ether as extraction agent in the inventive method should be selected from the saturated alkyl chloride of dechlorination other substituent low-carbon (LC)s of outer nothing, as methylene dichloride, trichloromethane, tetracol phenixin, 1,2-ethylene dichloride, chlorobutane etc.The two-phase system that these organic solvents all can make itself and water form is realized separating of hexanolactam and diacetyl oxide, acetate by physical solvent extraction principle.
Method provided by the invention can adopt the intermittent mode operation, also can adopt the operating method of continuously feeding, discharging.The rearrangement reaction time is 0.01-2.0 hour, preferred 0.05-0.3 hour when adopting the intermittent mode operation; The rearrangement reaction time is 0.01-300 second when adopting the continuous mode operation.
Method provided by the invention has following advantage: the Beckmann rearrangement that (1) is efficient, highly selective has realized cyclohexanone-oxime prepares hexanolactam; (2) after rearrangement reaction finishes, obtain the hexanolactam of unbound state, without the ammoniacal liquor neutralization procedure, no sulphur ammonium by-product; (3) can realize recycling of catalyzer and organic solvent; (4) rearrangement reaction can be carried out in very wide temperature range and long time scope, realizes the control to speed of reaction easily.
Description of drawings
Fig. 1 is the process flow diagram of the inventive method.
Embodiment
Below in conjunction with embodiment technical scheme provided by the invention is further described, but not thereby limiting the invention.
Embodiment 1
The present embodiment explanation the present invention can implement in diacetyl oxide/toluene homogeneous system.
In the 100ml round-bottomed flask, add toluene 20.0ml successively, diacetyl oxide 3.0ml, 65 ℃ of oil bath temperature controls, magnetic agitation adds cyclohexanone-oxime/toluene solution 10.0ml of 2.0mol/L then, reacts after 30 minutes each amount of substance in the gas chromatographic analysis toluene solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 98.0%.
Embodiment 2
The present embodiment explanation the present invention can implement in diacetyl oxide/benzene homogeneous system.
In the 100ml round-bottomed flask, add 20.0ml benzene successively, diacetyl oxide 3.0ml, 65 ℃ of oil bath temperature controls, magnetic agitation adds cyclohexanone-oxime/benzole soln 10.0m1 of 2.0mol/L then, reacts after 20 minutes each amount of substance in the gas chromatographic analysis toluene solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 97.1%.
Embodiment 3
The present embodiment explanation the present invention can implement in diacetyl oxide/dimethylbenzene homogeneous system.
In the 100ml round-bottomed flask, add dimethylbenzene 20.0ml successively, diacetyl oxide 3.0ml, 65 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/xylene solution the 10.0ml that adds 2.0mol/L then reacts after 120 minutes each amount of substance in the gas chromatographic analysis toluene solution.Analytical results shows that the transformation efficiency of cyclohexanone-oxime is 100%, and the selectivity of hexanolactam is 94.3%.
Embodiment 4
The present embodiment explanation the present invention can implement in acetic anhydride/acetic acid ethyl ester homogeneous system.
In the 100ml round-bottomed flask, add ethyl acetate 20.0ml successively, diacetyl oxide 3.0ml, 65 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/ethyl acetate solution the 20.0ml that adds 1.0mol/L then reacts after 2.0 minutes each amount of substance in the gas chromatographic analysis ethyl acetate solution.The result shows that the transformation efficiency of cyclohexanone-oxime reaches 100.0%, and the selectivity of hexanolactam is 96.2%.
Embodiment 5
The present embodiment explanation the present invention can implement in diacetyl oxide/trichloromethane homogeneous system.
In the 100ml round-bottomed flask, add trichloromethane 20.0ml successively, diacetyl oxide 3.0ml, 65 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/chloroform soln the 10.0ml that adds 2.0mol/L then reacts after 2.0 hours each amount of substance in the gas chromatographic analysis chloroform soln.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 97.0%.
Embodiment 6
The present embodiment explanation the present invention can implement in diacetyl oxide/tetracol phenixin homogeneous system.
In the 100ml round-bottomed flask, add tetracol phenixin 20.0ml successively, diacetyl oxide 3.6ml, 60 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/carbon tetrachloride solution the 20.0ml that adds 1.0mol/L then reacts after 2.0 minutes each amount of substance in the gas chromatographic analysis carbon tetrachloride solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 94.9%.
Embodiment 7
The present embodiment explanation the present invention can implement in diacetyl oxide/n-hexyl alcohol homogeneous system.
In the 100ml round-bottomed flask, add n-hexyl alcohol 20.0ml successively, diacetyl oxide 3.6ml, 60 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/n-hexyl alcohol solution the 6.0ml that adds 4.0mol/L then reacts after 20 minutes each amount of substance in the gas chromatographic analysis n-hexyl alcohol solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 99.8%, and the selectivity of hexanolactam is 97.7%.
Embodiment 8
The present embodiment explanation the present invention can implement in diacetyl oxide/ether homogeneous system.
In the 100ml round-bottomed flask, add ether 4.0ml successively, diacetyl oxide 16.0ml, 35 ℃ of oil bath temperature controls, magnetic agitation adds cyclohexanone-oxime/diethyl ether solution 15.0ml of 2.0mol/L then, reacts after 10 minutes each amount of substance in the gas chromatographic analysis diethyl ether solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 83.2%.
Embodiment 9
Present embodiment explanation the present invention can use diacetyl oxide and acetate mixture to implement as catalyzer.
In the 100ml round-bottomed flask, add dimethylbenzene 20.0ml successively, diacetyl oxide 3.0ml and Glacial acetic acid 0.6ml, 30 ℃ of oil bath temperature controls, magnetic agitation, add 2.0mol/L cyclohexanone-oxime/toluene solution 10.0ml then, react after 20 minutes each amount of substance in the gas chromatographic analysis xylene solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 96.8%.
Embodiment 10
Present embodiment explanation the present invention can adopt lower oxime strength of solution to implement.
In the 100ml round-bottomed flask, add toluene 20.0ml successively, diacetyl oxide 3.0ml, 65 ℃ of oil bath temperature controls, magnetic agitation adds cyclohexanone-oxime/toluene solution 10.0ml of 0.2mol/L then, reacts after 20 minutes each amount of substance in the gas chromatographic analysis toluene solution.The result shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 94.4%.Crossing low oxime strength of solution can increase the volume of material handling, thereby reduces the economic feasibility of technology.
Embodiment 11
Present embodiment explanation the present invention can implement in diacetyl oxide/toluene system of 2%.
In the 100ml round-bottomed flask, add toluene 20.0ml successively, diacetyl oxide 0.40ml, 80 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/toluene solution the 10.0ml that adds 2.0mol/L then reacts after 30 minutes each amount of substance in the gas chromatographic analysis toluene solution.Analytical results shows that the transformation efficiency of cyclohexanone-oxime is 16.5%, and the selectivity of hexanolactam is 80.4%.Can reduce the selectivity of hexanolactam than low acetate acid anhydride concentration.
Embodiment 12
Present embodiment explanation the present invention can implement in diacetyl oxide/toluene system of 80%.In the 100ml round-bottomed flask, add toluene 5.0ml successively, diacetyl oxide 20.0ml, 110 ℃ of oil bath temperature controls, magnetic agitation, cyclohexanone-oxime/toluene solution the 10.0ml that adds 2.0mol/L then reacts after 30 minutes each amount of substance in the gas chromatographic analysis toluene solution.Analytical results shows that the transformation efficiency of cyclohexanone-oxime is 100.0%, and the selectivity of hexanolactam is 82.8%.
Embodiment 13
Present embodiment explanation tributyl phosphate (TBP) can pass through complexometric extraction principle extracting and separating hexanolactam and acetate effectively from the aqueous solution.
At first, in 100ml tool plug triangular flask, add the aqueous solution 30ml that contains 10% (V/V) acetate and 10% (W/V) hexanolactam, add TBP30ml then, at room temperature magnetic agitation is 1.5 hours, static phase-splitting in the separating funnel, the gas chromatographic analysis TBP and the aqueous solution are determined the content of each material in the solution with marker method.The result shows that 95.4% hexanolactam is retained in water, and promptly hexanolactam is 0.0482 at the partition ratio of TBP/ water two-phase system; 36.9% acetate is retained in water, and promptly acetate is 1.71 at the partition ratio of this two-phase system.Hexanolactam and acetate are 35.5 at the separation factor of this two-phase system, can effectively realize separating of hexanolactam and acetate.
Embodiment 14
Present embodiment explanation tributyl phosphate (TBP)/sherwood oil (b.p.:90-120 ℃) solution can extract principle extracting and separating hexanolactam and acetate effectively from the aqueous solution by complexing solvent.
At first, in 100ml tool plug triangular flask, add the aqueous solution 30ml that contains 10% (V/V) acetate and 10% hexanolactam (W/V), add 75%TBP/ petroleum ether solution 30ml then, at room temperature magnetic agitation is 1.5 hours, static phase-splitting in the separating funnel, the gas chromatographic analysis organic phase and the aqueous solution are determined the content of each material in the solution with marker method.The result shows that 95.6% hexanolactam is retained in water, and promptly hexanolactam is 0.0460 at the partition ratio of this profit two-phase system; 46.0% acetate is retained in water, and promptly acetate is 1.174 at the partition ratio of this profit two-phase system.Hexanolactam and acetate are 25.5 at the separation factor of TBP-sherwood oil/water two-phase system, easily effectively realize separating of hexanolactam and acetate by the extraction of 3-4 level.
Embodiment 15
The present embodiment explanation can use trichloromethane to go out hexanolactam by physical solvent extraction principle extracting and separating from the aqueous solution, and acetate is retained in water, thereby effectively realizes separating of hexanolactam and acetate.
At first, in 100ml tool plug triangular flask, add the aqueous solution 30ml that contains 10% (V/V) acetate and 10% hexanolactam (W/V), add trichloromethane 30ml then, at room temperature magnetic agitation is 1.5 hours, static phase-splitting in the separating funnel, the gas chromatographic analysis trichloromethane mutually and the aqueous solution is determined the content of each material in the solution with marker method.The result shows that 88.6% hexanolactam enters the trichloromethane phase, and promptly hexanolactam is 7.77 at the partition ratio of trichloromethane/aqueous systems; 69.5% acetate is retained in water, and promptly acetate is 0.439 at the partition ratio of trichloromethane/aqueous systems.Hexanolactam and the acetate separation factor in trichloromethane/aqueous systems is up to 17.7, effectively realizes separating of hexanolactam and acetate by the extraction of 3-4 level easily.
Claims (11)
1, a kind of method for preparing hexanolactam is with organic solvent and the mixed homogeneous phase solution of acetic anhydride that gets of diacetyl oxide; Under the rearrangement reaction temperature, will carry out the homogeneous phase rearrangement reaction in cyclohexanone-oxime or its solution adding solution of acetic anhydride; Liquid phase after the water extraction rearrangement reaction, acquisition contains the water of hexanolactam, diacetyl oxide and acetate, and organic solvent recycles after handling; Use the extraction agent aqueous phase extracted, the realization hexanolactam separates with diacetyl oxide and acetate; Hexanolactam enters FF; Diacetyl oxide and acetate recycle after changing into diacetyl oxide.
2, in accordance with the method for claim 1, wherein said organic solvent is selected from benzene,toluene,xylene, trimethylbenzene, propyl carbinol, hexanol, octanol, ether, n-butyl ether, ethyl acetate, butylacetate, pentyl acetate, methylene dichloride, trichloromethane, tetracol phenixin, 1, one of 2-ethylene dichloride, chlorobutane, acetate, propionic acid, butyric acid, caproic acid.
3, in accordance with the method for claim 1, wherein said in the solution of acetic anhydride of organic solvent and diacetyl oxide composition, the volumetric concentration of diacetyl oxide is 1.0%-80%.
4, in accordance with the method for claim 3, in the wherein said solution of acetic anhydride, the volumetric concentration of diacetyl oxide is 10%-30%.
5, in accordance with the method for claim 1, wherein said rearrangement reaction temperature is the boiling point of room temperature to organic solvent.
6, in accordance with the method for claim 5, wherein said rearrangement reaction temperature is 40-80 ℃.
7, in accordance with the method for claim 1, the mol ratio of wherein said cyclohexanone-oxime and diacetyl oxide consumption is 1: (1.0-3.0).
8, in accordance with the method for claim 7, the mol ratio of wherein said cyclohexanone-oxime and diacetyl oxide consumption is 1: (1.3-2.0).
9, in accordance with the method for claim 1, wherein said extraction agent is the neutral phosphorus-based extractant that is selected from tributyl phosphate, trioctyl phosphate, tricresyl phosphate alkane ester, TRPO.
10, according to claim 1 or 9 described methods, wherein said extraction agent be dissolved in the organic solvent of one of normal hexane, normal heptane, octane-iso, sherwood oil, benzene,toluene,xylene, volumetric concentration is the neutral phosphorus-based extractant solution of 10-95%.
11, in accordance with the method for claim 1, wherein said extraction agent is for being selected from methylene dichloride, trichloromethane, tetracol phenixin, 1, the saturated hydrochloric ether of the low-carbon (LC) of one of 2-ethylene dichloride, chlorobutane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100886964A CN100363351C (en) | 2004-11-17 | 2004-11-17 | Production of hexyl lactam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100886964A CN100363351C (en) | 2004-11-17 | 2004-11-17 | Production of hexyl lactam |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1778795A true CN1778795A (en) | 2006-05-31 |
| CN100363351C CN100363351C (en) | 2008-01-23 |
Family
ID=36769259
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100886964A Active CN100363351C (en) | 2004-11-17 | 2004-11-17 | Production of hexyl lactam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100363351C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101117327B (en) * | 2006-07-31 | 2010-09-22 | 中国石油化工股份有限公司 | Preparation method of aminocaprolactam |
| CN102863385A (en) * | 2012-10-09 | 2013-01-09 | 清华大学 | Method for directly synthesizing caprolactam through cyclohexanone |
| CN102895996A (en) * | 2012-10-09 | 2013-01-30 | 清华大学 | Catalytic system for Beckmann rearrangement of oxime |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH394212A (en) * | 1962-01-13 | 1965-06-30 | Inventa Ag | Process for rearrangement of cyclic oximes |
-
2004
- 2004-11-17 CN CNB2004100886964A patent/CN100363351C/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101117327B (en) * | 2006-07-31 | 2010-09-22 | 中国石油化工股份有限公司 | Preparation method of aminocaprolactam |
| CN102863385A (en) * | 2012-10-09 | 2013-01-09 | 清华大学 | Method for directly synthesizing caprolactam through cyclohexanone |
| CN102895996A (en) * | 2012-10-09 | 2013-01-30 | 清华大学 | Catalytic system for Beckmann rearrangement of oxime |
| CN102895996B (en) * | 2012-10-09 | 2014-11-26 | 清华大学 | Catalytic system for Beckmann rearrangement of oxime |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100363351C (en) | 2008-01-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101117327B (en) | Preparation method of aminocaprolactam | |
| CN102040606B (en) | Synthetic method of vinpocetine | |
| CN201719863U (en) | Wet phosphoric acid extraction and purification device | |
| CN1830762A (en) | Method of continuously preparing potassium dihydrogen phosphate | |
| CN105152980A (en) | Chiral preparation method for N-t-butyloxycarboryl-(4S)-(p-phenyl phenyl methyl)-4-amino-(2R)-methylbutyric acid | |
| CN1778796A (en) | Production of hexyl lactam in ion liquid | |
| CN102304163A (en) | Fluorous synthesis method of betamethasone | |
| CN1778795A (en) | Production of hexyl lactam | |
| CN105964306A (en) | Poly(ionic liquid)-based magnetic nanoparticle and its preparation method and use in three-ingredient reaction | |
| CN103788069A (en) | Preparation method for esomeprazole magnesium trihydrate | |
| CN101597277B (en) | Novel method for preparing S-pantoprazole and salt | |
| CN102531299B (en) | Method for treating addition wastewater in production process of lipoic acid | |
| CN103193800B (en) | A kind of method of each component of separation and purification from cefaclor enzymatic reaction liquid | |
| CN1680254A (en) | Oxosynthesis of azelaic acid and nonoic acid with mixed ozone solvent | |
| CN1439630A (en) | Extraction of natural capsaicine | |
| CN101812107A (en) | Method for synthesizing clobetasol propionate intermediate | |
| CN1670017A (en) | Method for separating Beckmann rearrangement reaction products from ion liquid | |
| CN1238262C (en) | Process for separating and recovering minim organic solvent from waste water using ion liquid | |
| CN111939978A (en) | Preparation method and application of heterogeneous metal catalyst | |
| CN1294119C (en) | Method for synthesizing bifunctionality initiator DIOOH | |
| CN102134251A (en) | Method for extracting cephalosporin C by using water soluble organic solvent/salt/water two-phase system | |
| CN106316755A (en) | Method for treating waste sulfuric acid through extraction separation coupled ammonium chloride reaction | |
| CN105195228A (en) | Fe3O4-loaded chiral catalyst and preparation method and application thereof | |
| CN1185191C (en) | Process for preparation of alicyclic ketones and alkyl-substituted alicyclic esters | |
| CN1121409C (en) | Process for preparing medicine |
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 |