CN106866431A - A kind of production method of 1,3 propane diamine of N (2 methoxycyclohexyl) - Google Patents
A kind of production method of 1,3 propane diamine of N (2 methoxycyclohexyl) Download PDFInfo
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- CN106866431A CN106866431A CN201710095091.5A CN201710095091A CN106866431A CN 106866431 A CN106866431 A CN 106866431A CN 201710095091 A CN201710095091 A CN 201710095091A CN 106866431 A CN106866431 A CN 106866431A
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- methoxycyclohexyls
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C213/00—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C213/00—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton
- C07C213/08—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton by reactions not involving the formation of amino groups, hydroxy groups or etherified or esterified hydroxy groups
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C213/00—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton
- C07C213/10—Separation; Purification; Stabilisation; Use of additives
Abstract
The invention discloses a kind of synthesis of compound, separation method, a kind of production method of the propane diamine of N (2 methoxycyclohexyl) 1,3 is specifically referred to.It with 3 (2 methoxycyclohexyl) aminopropionitriles is raw material that the present invention is, hydrogenated synthesis and separated removal incoagulable gas and water etc. low-boiling-point substance and come, then feed separation is carried out through different knockout towers, obtain purity product higher, it is an advantage of the invention that having obtained the N (2 methoxycyclohexyl) 1 of high-quality, 3 propane diamine products, and various materials obtained fully, effective utilize.This method separation process simplicity, energy consumption, consumption of raw materials are low, and the good product quality rate of recovery is high, low production cost.
Description
Technical field
The present invention relates to a kind of synthesis of compound, separation method, a kind of N- (2- methoxycyclohexyls) -1 is specifically referred to,
The separation method of 3- propane diamine.
Background technology
N- (2- methoxycyclohexyls) -1,3- propane diamine is a kind of important organic chemical industry's intermediate, as epoxy resin
Curing agent and modified firming agent raw material, be also used as polymerization auxiliary agent and rubber additive, also can be used as production medicine,
The intermediate of agricultural chemicals.Molecular formula：C10H22N2O, molecular weight：186.29.As a kind of new organic chemical industry's intermediate, it is given birth to
(synthesis, separation) method existing document is produced not relate to also and report.
The content of the invention
The present inventor completes the present invention by substantial amounts of research work.
It is an object of the invention to provide a kind of flow advantages of simple, low production cost, good product quality is adapted to industrial production
N- (2- methoxycyclohexyls) -1,3- propane diamine continuous production method.
The continuous production method of N- (2- methoxycyclohexyls) -1,3- propane diamine be with 3- (2- methoxycyclohexyls) -
Aminopropionitrile is raw material, the low-boiling-point substance such as hydrogenated synthesis and separated removal incoagulable gas and water and come, i.e., institute of the present invention
For N- (2- methoxycyclohexyls) -1,3- propane diamine synthetic routes be 3- (2- methoxycyclohexyls)-aminopropionitrile route,
Can be containing part 2- methoxycyclohexyls amine and a small amount of in its raw material 3- (2- methoxycyclohexyls)-aminopropionitrile material system
Organic compound containing unsaturated bonds such as-C=C- ,-C ≡ C- ,-C ≡ N.
Other impurities can be methyl alcohol, 1,3- propane diamine and raw material in intending separate mixture A in above-mentioned technical proposal
The medium organic compound hydrogenation reaction containing unsaturated bonds such as-C=C- ,-C ≡ C- ,-C ≡ N and come material.
The present invention is to solve its technical problem by following technical proposals：
A kind of production method of N- (2- methoxycyclohexyls) -1,3- propane diamine, it is characterised in that comprise the steps：
(1) with 3- (2- methoxycyclohexyls)-aminopropionitrile as raw material, the mixture obtained by hydrogenated synthesis；Will be above-mentioned
Mixture is separated into Light ends knockout tower, from low boiling impurity, first containing 2- such as overhead extraction cyclohexyl methyl ether, 1,3- propane diamine
Epoxide cyclohexylamine, N- cyclohexyl -1,3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls
Base) mixture of a small amount of high-boiling components such as-aminopropionitrile separated from tower reactor into methoxycyclohexyl amine recovery tower middle part；
(2) material of methoxycyclohexyl amine recovery tower is entered, it is separated, from overhead extraction 2- methoxycyclohexyl amine products,
- the 1,3- of cyclohexyl containing N- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls)-aminopropan
The mixture of a small amount of high-boiling components such as nitrile enters product knockout tower from middle part；
(3) enter product knockout tower material, it is separated after, from overhead extraction N- (2- methoxycyclohexyls) -1,3- third
Two amine products, tower reactor is the high-boiling components containing a small amount of N- (2- methoxycyclohexyls) -1,3- propane diamine products；Wherein product is separated
The number of plates of tower is 40~60 pieces, and rectifying section is 15~35 blocks of column plates, and tower top temperature is 100~160 DEG C, and bottom temperature is 120
~180 DEG C, tower top pressure -0.0998MPa<P≤0MPa, overhead reflux liquid reflux ratio is 4~10；
Preferably, N- (2- methoxycyclohexyls) -1, the 3- propane diamine product knockout towers described in aforementioned production method
Tower top pressure is -0.0998MPa<P≤-0.09MPa.Be due to N- (2- methoxycyclohexyls) -1,3- propane diamine product in itself
The reason for physical property, show it is more sensitive to the change of pressure-temperature, because compound composition produced in organic reaction is multiple
It is miscellaneous, so choosing the operating conditions such as accurate temperature, pressure, can not only obtain good separating effect, it is also possible to realizationization
Learn the suitable control of byproduct of reaction；So seeming extremely important for the control such as pressure herein.
Preferably, the methoxycyclohexyl amine recovery tower described in aforementioned production method is vacuumizing, it is due to mixing
Objects system material in itself physical property the reason for, show it is more sensitive to the change of pressure-temperature, even if being that this is relatively low in pressure
In the case of, with.
Preferably, separation process system carries out closed cycle in aforementioned production method, Matter Transfer is utilized.
Preferably, Light ends knockout tower described in aforementioned production method, methoxycyclohexyl amine recovery tower, product knockout tower
Using calendering acanthopore mellapak packing tower, the feed rate of each tower is controlled in 4000 kgs/hr of every square metre of tower sections
Within product.
Preferably, in the mixture for entering methoxycyclohexyl amine tower in step (2) in aforementioned production method, not including
The low-boiling-point substance mass content of 2- methoxycyclohexyl amine is controlled within 0.05%.
Preferably, in aforementioned production method in the middle material for entering product knockout tower of step (3), cyclohexyl containing N- -1,
3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, the high-boiling components of 3- (2- methoxycyclohexyls)-aminopropionitrile are mixed
The mass content of compound is controlled more than 99.5%.
In this application, due to certainly existing the accessory substances such as some incomplete reactants in organic synthesis, so will
Containing cyclohexyl methyl ether, propylamine, 2- methoxycyclohexyls amine, N- cyclohexyl -1,3- propane diamine, N- (2- methoxycyclohexyls) -
The mixture of the high-boiling components such as 1,3- propane diamine, 3- (2- methoxycyclohexyls)-aminopropionitrile and a small amount of other impurities (referred to as mixes
Thing A) enter Light ends knockout tower middle part, it is separated, from low boiling impurity such as overhead extraction cyclohexyl methyl ether, propylamine；First containing 2-
Epoxide cyclohexylamine, N- cyclohexyl -1,3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls
Base) mixture (abbreviation mixture B) of a small amount of high-boiling components such as-aminopropionitrile carries out from tower reactor into methoxycyclohexyl amine tower middle part
Separate, now generally low-boiling-point substance≤0.05% before 2- methoxycyclohexyls amine (not including) in mixture B.It is separated,
From the 2- methoxycyclohexyl amine of overhead extraction content more than 99.5%, cyclohexyl containing N- -1,3- propane diamine, N- (2- methoxy basic rings
Hexyl) a small amount of high-boiling components such as -1,3- propane diamine, 3- (2- methoxycyclohexyls)-aminopropionitrile mixture (abbreviation mixture C)
Into product knockout tower, now 2- methoxycyclohexyls amine content≤0.5% in mixture C；Mixture C is separated, from product tower
Top extraction content is more than 99.5% N- (2- methoxycyclohexyls) -1,3- propane diamine products, and tower reactor is high-boiling components.Whole point
From the total low boiling impurity knockout tower of flow, methoxycyclohexyl amine tower, three knockout towers of product knockout tower, the form of knockout tower can be with
It is valve tower, bubble column, packed tower, but is optimal, feed rate≤4,000,000 of each tower to roll acanthopore mellapak packing tower
Gram/(every square metre of tower section product of hour).Wherein the number of plates of product knockout tower is 40~60 pieces, and rectifying section is 15~35 pieces
Column plate, tower top temperature is 100~160 DEG C, and bottom temperature is 120~180 DEG C, and tower top pressure is less than or equal to more than -0.0998
0MPa, overhead reflux liquid reflux ratio is 4~10.In this application, described low-boiling-point substance, high-boiling components are known normal in industry
Know, so no longer enumerating formula explanation to this.
The invention has the advantages that：N- (2- methoxycyclohexyls) -1, the 3- propane diamine products of high-quality have been obtained, and
And various materials have obtained fully, effectively utilizing.This method separation process simplicity, energy consumption, consumption of raw materials are low, good product quality
The rate of recovery is high, low production cost.
Specific embodiment
Implementation of the invention is illustrated below：
Embodiment 1：
A kind of production method of N- (2- methoxycyclohexyls) -1,3- propane diamine, comprises the steps：
(1) with 3- (2- methoxycyclohexyls)-aminopropionitrile as raw material, the mixture obtained by hydrogenated synthesis；Will be above-mentioned
Mixture is separated into Light ends knockout tower, from low boiling impurity, first containing 2- such as overhead extraction cyclohexyl methyl ether, 1,3- propane diamine
Epoxide cyclohexylamine, N- cyclohexyl -1,3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls
Base) mixture of a small amount of high-boiling components such as-aminopropionitrile separated from tower reactor into methoxycyclohexyl amine recovery tower middle part；
(2) material of methoxycyclohexyl amine recovery tower is entered, it is separated, from overhead extraction 2- methoxycyclohexyl amine products,
- the 1,3- of cyclohexyl containing N- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls)-aminopropan
The mixture of a small amount of high-boiling components such as nitrile enters product knockout tower from middle part；
(3) enter product knockout tower material, it is separated after, from overhead extraction N- (2- methoxycyclohexyls) -1,3- third
Two amine products, tower reactor is the high-boiling components containing a small amount of N- (2- methoxycyclohexyls) -1,3- propane diamine products；Wherein product is separated
The number of plates of tower is 40~60 pieces, and rectifying section is 15~35 blocks of column plates, and tower top temperature is 100~160 DEG C, and bottom temperature is 120
~180 DEG C, tower top pressure -0.0998MPa<P≤0MPa, overhead reflux liquid reflux ratio is 4~10；
In the present embodiment, mixture A enters the piece-rate system of tower a diameter of 100 with about 50 kgs/hr of flow, and this is mixed
The weight composition of each component is as follows in compound：Cyclohexyl methyl ether 1.1%, 1,3- propane diamine 0.7%, other Light ends
1.65%th, 2- methoxycyclohexyls amine 15.95%, N- cyclohexyl -1,3- propane diamine 0.1%, N- (2- methoxycyclohexyls) -1,3-
Propane diamine 78.79%, 3- (2- methoxycyclohexyls)-aminopropionitrile and high-boiling components 1.71%.Mixture A is separated through Light ends
Tower separates the Light ends such as tower top removal cyclohexyl methyl ether, 1,3- propane diamine, and kettle material mixture B is through methoxycyclohexyl amine tower
Separate, the 2- methoxycyclohexyl amine of overhead extraction more than 99.5%, kettle material is mixture C.The weight of each component in mixture C
Amount composition is as follows：2- methoxycyclohexyls amine 0.25%, N- cyclohexyl -1,3- propane diamine 0.09%, N- (2- methoxycyclohexyls) -
1,3- propane diamine 97.55%, 3- (2- methoxycyclohexyls)-aminopropionitrile and high-boiling components 2.11%.The mixture C enters product
Knockout tower middle part, 40.385 kgs/hr of flow, product knockout tower is calendering acanthopore mellapak packing tower, has 55 pieces of column plate.
Wherein 32 pieces of rectifying section, tower top pressure is -0.0995MPa, and tower top temperature is 110 DEG C, and bottom temperature is 124 DEG C, overhead reflux
Liquid reflux ratio is 4.Product knockout tower overhead extraction mass flow is 39.475 kgs/hr, wherein N- (2- methoxycyclohexyls
Base) -1,3- propane diamine mass content be 99.59%, high-boiling components are 0.06%；Product knockout tower bottom of towe produces mass flow
0.91 kg/hr, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 8.79%.
Embodiment 2：
By the condition and step of embodiment 1, it is -0.097MPa to change product knockout tower tower top pressure, and tower top temperature is 144
DEG C, bottom temperature is 160 DEG C, and overhead reflux liquid reflux ratio is 4.Product knockout tower overhead extraction mass flow be 39.5 kilograms/
Hour, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 99.53%, and high-boiling components are 0.13%；Product point
It it is 0.885 kg/hr from tower bottom of towe extraction mass flow, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine quality contains
Measure is 9.04%.
Embodiment 3：
By the condition and step of embodiment 1, it is -0.092MPa only to change product knockout tower tower top pressure, and tower top temperature is
170 DEG C, bottom temperature is 190 DEG C, and overhead reflux liquid reflux ratio is 4.Product knockout tower overhead extraction mass flow is 39.435
Kg/hr, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 99.28%, and high-boiling components are 0.38%；
Product knockout tower bottom of towe extraction mass flow is 1.9 kgs/hr, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine matter
Amount content is 25.79%.
Embodiment 4：
By the condition and step of embodiment 1, it is -0.092MPa only to change product knockout tower tower top pressure, and tower top temperature is
170 DEG C, bottom temperature is 190 DEG C, and overhead reflux liquid reflux ratio is 10.Product knockout tower overhead extraction mass flow is 39.49
Kg/hr, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 99.52%, and high-boiling components are 0.14%；
Product knockout tower bottom of towe extraction mass flow is 0.995 kg/hr, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine
Mass content is 24.62%.
Embodiment 5：
By the condition and step of embodiment 1, only change product knockout tower tower height degree, 48 pieces of total number of plates.Wherein rectifying section
28 pieces.Product knockout tower overhead extraction mass flow is 39.42 kgs/hr, wherein N- (2- methoxycyclohexyls) -1,3- third
Diamines mass content is 99.51%, and high-boiling components are 0.49%；Product knockout tower bottom of towe extraction mass flow be 0.965 kilogram/it is small
When, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 17.62%.
Embodiment 6：
By the condition and step of embodiment 1, it is -0.092MPa to change product knockout tower tower top pressure, and tower top temperature is 170
DEG C, bottom temperature is 190 DEG C, and overhead reflux liquid reflux ratio is 10, and methoxycyclohexyl amine recovery tower is vacuumizing, separation process
System carries out closed cycle, and Matter Transfer is utilized, and is entered in step (2) in the mixture of methoxycyclohexyl amine tower, not comprising 2-
The low-boiling-point substance mass content of methoxycyclohexyl amine is controlled within 0.05%.Product knockout tower overhead extraction mass flow is
39.49 kgs/hr, wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 99.52%, and high-boiling components are
0.14%；Product knockout tower bottom of towe extraction mass flow is 0.995 kg/hr, wherein N- (2- methoxycyclohexyls) -1,3-
Propane diamine mass content is 23.78%.
Embodiment 7：
By the condition and step of embodiment 6, it is -0.092MPa to change product knockout tower tower top pressure, and tower top temperature is 170
DEG C, bottom temperature is 190 DEG C, and overhead reflux liquid reflux ratio is 10, and methoxycyclohexyl amine recovery tower is vacuumizing, separation process
System carries out closed cycle, and Matter Transfer is utilized, in the material for entering product knockout tower in step (3), cyclohexyl containing N- -1,
3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, the high-boiling components of 3- (2- methoxycyclohexyls)-aminopropionitrile are mixed
The mass content of compound is controlled more than 99.5%.Product knockout tower overhead extraction mass flow is 39.49 kgs/hr, its
Middle N- (2- methoxycyclohexyls) -1,3- propane diamine mass content is 99.52%, and high-boiling components are 0.14%；Product knockout tower tower
Bottom extraction mass flow is 0.995 kg/hr, and wherein N- (2- methoxycyclohexyls) -1,3- propane diamine mass contents are
24.12%.
The present invention be applied to 3- (2- methoxycyclohexyls)-aminopropionitrile hydrogenation method route N- (2- methoxycyclohexyls)-
The separating-purifying of 1,3- propane diamine but it is not limited to 3- (2- methoxycyclohexyls)-aminopropionitrile hydrogenation method route N- (2- methoxies
Butylcyclohexyl) -1,3- propane diamine separation, be equally applicable to other and finally add through 3- (2- methoxycyclohexyls)-aminopropionitrile
The separation of N- (2- methoxycyclohexyls) -1, the 3- propane diamine of hydrogen synthetic route, with reference to the method for the invention, by adjusting,
Changing the partial parameters in operating condition of the present invention can realize that other are final through 3- (2- methoxycyclohexyls)-aminopropionitrile
The separation of N- (2- methoxycyclohexyls) -1,3- propane diamine of hydrogenation synthesis route.
For those skilled in the art, it is aobvious that the present invention carries out various modifications and variations (change of material content)
And be clear to, and it is construed as such modifications and variations all within the scope of this specification, also appended claim
Spirit and scope within.
Claims (7)
1. a kind of production method of N- (2- methoxycyclohexyls) -1,3- propane diamine, it is characterised in that comprise the steps：
(1) with 3- (2- methoxycyclohexyls)-aminopropionitrile as raw material, the mixture obtained by hydrogenated synthesis；By above-mentioned mixing
Thing is separated into Light ends knockout tower, from low boiling impurity, methoxyl group containing 2- such as overhead extraction cyclohexyl methyl ether, 1,3- propane diamine
Cyclohexylamine, N- cyclohexyl -1,3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls) -
The mixture of a small amount of high-boiling components such as aminopropionitrile is separated from tower reactor into methoxycyclohexyl amine recovery tower middle part；
(2) material of methoxycyclohexyl amine recovery tower is entered, it is separated, from overhead extraction 2- methoxycyclohexyl amine products, containing N-
Cyclohexyl -1,3- propane diamine, N- (2- methoxycyclohexyls) -1,3- propane diamine, 3- (2- methoxycyclohexyls)-aminopropionitrile etc.
The mixture of a small amount of high-boiling components enters product knockout tower from middle part；
(3) enter product knockout tower material, it is separated after, from overhead extraction N- (2- methoxycyclohexyls) -1,3- propane diamine
Product, tower reactor is the high-boiling components containing a small amount of N- (2- methoxycyclohexyls) -1,3- propane diamine products；Wherein product knockout tower
The number of plates is 40~60 pieces, and rectifying section is 15~35 blocks of column plates, and tower top temperature is 100~160 DEG C, and bottom temperature is 120~180
DEG C, tower top pressure -0.0998MPa<P≤0MPa, overhead reflux liquid reflux ratio is 4~10.
2. the production method of N- (2- methoxycyclohexyls) -1,3- propane diamine according to claim 1, it is characterised in that institute
N- (2- the methoxycyclohexyls) -1,3- propane diamine product knockout towers tower top pressure stated is -0.0998MPa<P≤-0.09MPa.
3. the production method of N- (2- methoxycyclohexyls) -1,3- propane diamine according to claim 1, it is characterised in that institute
The methoxycyclohexyl amine recovery tower stated is vacuumizing.
4. the production method of N- (2- methoxycyclohexyls) -1,3- propane diamine according to claim 1, it is characterised in that institute
The separation process system stated carries out closed cycle, and Matter Transfer is utilized.
5. the production method of N- (2- methoxycyclohexyls) -1,3- propane diamine according to claim 1, it is characterised in that institute
Light ends knockout tower, methoxycyclohexyl amine recovery tower, product knockout tower are stated using calendering acanthopore mellapak packing tower, each tower
Feed rate control is within 4000 kgs/hr of every square metre of tower section products.
6. the production method of N- (2- methoxycyclohexyls) -1,3- propane diamine according to claim 1, it is characterised in that
Enter in step (2) in the mixture of methoxycyclohexyl amine tower, the low-boiling-point substance mass content control not comprising 2- methoxycyclohexyl amine
System is within 0.05%.
7. the production method of N- (2- methoxycyclohexyls) -1,3- propane diamine according to claim 1, it is characterised in that step
Suddenly enter in (3) in the material of product knockout tower, cyclohexyl containing N- -1,3- propane diamine, N- (2- methoxycyclohexyls) -1,3- third
Diamines, the mass content of the high-boiling components mixture of 3- (2- methoxycyclohexyls)-aminopropionitrile are controlled more than 99.5%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107941976A (en) * | 2017-09-28 | 2018-04-20 | 浙江新化化工股份有限公司 | A kind of content assaying method of 2 methoxycyclohexyl amine |
| CN109725070A (en) * | 2017-10-31 | 2019-05-07 | 浙江新化化工股份有限公司 | A kind of content assaying method of N- (2- methoxycyclohexyl) -1,3- propane diamine |
| CN115108924A (en) * | 2022-06-24 | 2022-09-27 | 岳阳昌德新材料有限公司 | Amine intermediate and preparation method and application thereof |
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|---|---|---|---|---|
| CN1365965A (en) * | 2001-01-05 | 2002-08-28 | 巴斯福股份公司 | Method of preparing primary amine and secondary amine from nitrile |
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2017
- 2017-02-22 CN CN201710095091.5A patent/CN106866431B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1365965A (en) * | 2001-01-05 | 2002-08-28 | 巴斯福股份公司 | Method of preparing primary amine and secondary amine from nitrile |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107941976A (en) * | 2017-09-28 | 2018-04-20 | 浙江新化化工股份有限公司 | A kind of content assaying method of 2 methoxycyclohexyl amine |
| CN107941976B (en) * | 2017-09-28 | 2019-11-19 | 浙江新化化工股份有限公司 | A kind of content assaying method of 2- methoxycyclohexyl amine |
| CN109725070A (en) * | 2017-10-31 | 2019-05-07 | 浙江新化化工股份有限公司 | A kind of content assaying method of N- (2- methoxycyclohexyl) -1,3- propane diamine |
| CN109725070B (en) * | 2017-10-31 | 2022-05-10 | 浙江新化化工股份有限公司 | Method for measuring content of N- (2-methoxycyclohexyl) -1,3-propane diamine |
| CN115108924A (en) * | 2022-06-24 | 2022-09-27 | 岳阳昌德新材料有限公司 | Amine intermediate and preparation method and application thereof |
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