CN103012412B - Separation method of triethylene diamine and ethanolamine azeotrope - Google Patents
Separation method of triethylene diamine and ethanolamine azeotrope Download PDFInfo
- Publication number
- CN103012412B CN103012412B CN201210476478.2A CN201210476478A CN103012412B CN 103012412 B CN103012412 B CN 103012412B CN 201210476478 A CN201210476478 A CN 201210476478A CN 103012412 B CN103012412 B CN 103012412B
- Authority
- CN
- China
- Prior art keywords
- thanomin
- azeotrope
- tower
- entrainer
- triethylene diamine
- 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.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention aims at providing a separation method of triethylene diamine and ethanolamine azeotrope which has low use amount of an azeotrope former and small energy consumption. The separation method of triethylene diamine and ethanolamine azeotrope provided by the invention is carried out according to the following steps: (1) the azeotrope of triethylene diamine and ethanolamine and the azeotrope former are sent into an azeotropic distillation column, wherein an overhead fraction is azeotrope of the azeotrope former and ethanolamine, the tower kettle fraction is a mixture of triethylene diamine and azeotrope former, and the azeotrope former is bicyclohexyl or decalin; (2) the overhead fraction of the azeotropic distillation column enters a phase splitter to carry out phase separation, wherein the upper layer is the azeotrope former which is recycled to the azeotropic distillation column and the lower layer is an ethanolamine crude product which enters an ethanolamine refined tower; and (3) the overhead fraction of the ethanolamine refined tower is azeotrope of the azeotrope former and ethanolamine which is recycled to the azeotropic distillation column, and the tower kettle fraction of the ethanolamine refined tower is ethanolamine. The separation method of triethylene diamine and ethanolamine azeotrope provided by the invention can effectively reduce the use amount of the azeotrope former and obviously lower the energy consumption.
Description
Technical field
The invention belongs to the purification technique field of fine chemicals, relate to the separation method of a kind of triethylene diamine and thanomin azeotrope.
Background technology
Triethylene diamine is the whipping agent of producing flexible polyurethane, semihard, rigid foam, is also used to ethylene rolymerization catalyst, coating and plastics etc.
At present the raw materials of triethylene diamine be mainly N-hydroxyethyl piperazine, quadrol, thanomin,
Piperazine etc.Taking thanomin and liquefied ammonia during as catalytic material amination synthesis of ethylenediamine or piperazine, can coproduction triethylene diamine.Due to triethylene diamine (boiling point is 174 DEG C) and thanomin (boiling point is 170 DEG C) boiling point very approaching, both easily form azeotrope, adopt conventional rectification method to be difficult to both to separate, therefore, the triethylene diamine crude product that the method makes is the azeotrope of triethylene diamine and thanomin.
The separation method of the open triethylene diamine of CN201110430727.X and thanomin azeotrope.It is entrainer that the method adopts p-Xylol or ethylbenzene, separate the azeotrope of triethylene diamine and thanomin by heterogeneous azeotropic rectification, in entrainer and azeotrope, the mol ratio of thanomin is 8.1:1, obtaining triethylene diamine product in azeotropy rectification column tower reactor, is thanomin at thanomin treating tower tower reactor cut.When this patent adopts azeotropic distillation, dimethylbenzene or ethylbenzene recycle in a large number, have the problem that entrainer usage quantity is large, energy consumption is high.
Summary of the invention
For the deficiencies in the prior art, the object of the present invention is to provide a kind of entrainer usage quantity triethylene amine and thanomin azeotrope low, that consume energy little to obtain separation method.
In order to realize above-mentioned technical assignment, the present invention adopts following technical scheme to be achieved:
A separation method for triethylene diamine and thanomin azeotrope, the method is carried out according to following steps:
(1) by the azeotrope of triethylene diamine and thanomin, entrainer is sent into azeotropy rectification column, overhead fraction is the azeotrope of entrainer and thanomin, tower reactor cut is triethylene diamine and azeotropic agent composition, this mixture is separated out solid through cooling post crystallization, the solid obtaining is after filtering triethylene diamine product, described entrainer is bis cyclohexane, naphthane or sym-trimethylbenzene, thanomin and bis cyclohexane in azeotrope, the mol ratio of naphthane or sym-trimethylbenzene entrainer is 3:1～1:2, working pressure 5kPa～the 50kPa of azeotropy rectification column, tower top temperature is 100 DEG C～130 DEG C, tower reactor temperature is 130 DEG C～160 DEG C, reflux ratio is 0.5～4, .
(2) overhead fraction of azeotropy rectification column enters and divides mutually device to divide mutually, and upper strata is entrainer, is circulated to azeotropy rectification column, and lower floor is thanomin crude product, enters thanomin treating tower, and the described working pressure that divides mutually device is normal pressure, 25 DEG C～60 DEG C of service temperatures;
(3) overhead fraction of thanomin treating tower is the azeotrope of entrainer and thanomin, be circulated to azeotropy rectification column, thanomin treating tower tower reactor cut is thanomin, the wherein working pressure 5kPa～20kPa of thanomin treating tower, tower top temperature is 90 DEG C～120 DEG C, tower reactor temperature is 100 DEG C～130 DEG C, and reflux ratio is 0.5～3.
Described entrainer is bis cyclohexane, naphthane or sym-trimethylbenzene.
The separation method of triethylene diamine as above and thanomin azeotrope, the method is carried out according to following steps:
(1) azeotrope of triethylene diamine and thanomin, entrainer bis cyclohexane enter azeotropy rectification column, overhead fraction is the azeotrope of entrainer bis cyclohexane and thanomin, tower reactor cut is the mixture of triethylene diamine and entrainer bis cyclohexane, this mixture is separated out solid through cooling post crystallization, the solid obtaining is after filtering triethylene diamine product, in azeotrope, the mol ratio of thanomin and entrainer bis cyclohexane is 1:1.25, the working pressure of azeotropy rectification column is 20kPa, tower top temperature is 122.4 DEG C, tower reactor temperature is 145.8 DEG C, and reflux ratio is 1.5;
(2) overhead fraction of azeotropy rectification column enters and divides mutually device to divide mutually, and upper strata is entrainer bis cyclohexane, is circulated to azeotropy rectification column, and lower floor is thanomin crude product, enters thanomin treating tower, and the working pressure that wherein divides mutually device is normal pressure, 32 DEG C of service temperatures;
(3) overhead fraction of thanomin treating tower is the azeotrope of entrainer bis cyclohexane and thanomin, be circulated to azeotropy rectification column, the tower reactor cut of thanomin treating tower is thanomin, the wherein working pressure 10kPa of thanomin treating tower, tower top temperature is 106.5 DEG C, tower reactor temperature is 109.7 DEG C, and reflux ratio is 2.
Under 1atm pressure, in the azeotropic of p-Xylol and thanomin composition, mole fraction is respectively 0.8039 and 0.1961, in the azeotropic composition of bis cyclohexane and thanomin, mole fraction is respectively 0.1669 and 0.8331, and in the azeotropic composition of naphthane and thanomin, mole fraction is respectively 0.6926 and 0.3074.Compared with dimethylbenzene, taking bis cyclohexane or naphthane as entrainer, separate triethylene diamine and thanomin azeotrope by heterogeneous azeotropic rectification, and more thanomins of can carrying under one's arms, can significantly reduce entrainer usage quantity, reduce the internal circulating load of entrainer between azeotropy rectification column and thanomin treating tower, thereby reduce energy consumption.Therefore, the present invention has the following advantages:
1) the present invention utilizes bis cyclohexane, naphthane or sym-trimethylbenzene and thanomin to form heterogeneous azeotrope, destroy triethylene diamine-thanomin azeotropic system, adopt two rectifying tower of azeotropy rectification column and thanomin treating tower to separate the azeotrope of triethylene diamine and thanomin;
2) the present invention has effectively reduced entrainer usage quantity.Compared with dimethylbenzene entrainer, in azeotrope, the mol ratio of thanomin and bis cyclohexane, naphthane or sym-trimethylbenzene entrainer is 1:1.25;
3) the present invention has significantly reduced energy consumption.Need the external world that energy 7672.05kW is provided taking dimethylbenzene as entrainer, need the external world that energy 1963.53kW is provided taking bis cyclohexane as entrainer, in contrast Energy Intensity Reduction 74.4%.
Brief description of the drawings
Fig. 1 is the separation process scheme figure of triethylene diamine and thanomin azeotrope.
In figure, the implication of each label is: T1-azeotropy rectification column, and T2-thanomin treating tower, V1-divides device mutually, H1-tower reactor reboiler, H2-overhead condenser, H3-tower reactor reboiler, H4-overhead condenser, all the other number designations are pipeline.
Below in conjunction with drawings and Examples, particular content of the present invention is described in more detail.
Embodiment
Below provide specific embodiments of the invention, it should be noted that the present invention is not limited to following specific embodiment, all equivalents of doing on present techniques scheme basis all fall into protection scope of the present invention.
Logistics (the triethylene diamine 75g/h entering through pipeline 11, thanomin 25g/h) and logistics (the entrainer bis cyclohexane 400g/h that enters through pipeline 12, the mol ratio of entrainer and thanomin is 1.25:1) 69 DEG C of temperature from azeotropy rectification column T1(packing tower, tower diameter is Φ 25mm, the Stainless Steel Helices of in-built Φ 3*3 θ ring, bed stuffing height is 0.8m) middle part charging.
The overhead fraction of azeotropy rectification column T1 is the azeotrope of entrainer and thanomin, azeotrope is from pipeline 16, enter condenser H2, after cooling, enter through pipeline 17 that to divide mutually device V1(working pressure be normal pressure, service temperature is 32 DEG C), the upper strata of dividing mutually device V1 is entrainer phase, is circulated to T1 tower as backflow through pipeline 18, and the lower floor that divides mutually device V1 is thanomin crude product; Azeotropy rectification column T1 tower reactor cut is the mixture of triethylene diamine and entrainer, this mixture goes out from tower bottom flow through pipeline 15, a part enters reboiler H1 and circulates into azeotropy rectification column T1 circulating vaporization through pipeline 14, another part is after pipeline 13 is discharged, after cooling, crystallization, separate out solid, the solid phase prod obtaining after filtration is triethylene diamine product.
Thanomin crude product enters thanomin treating tower T2 through pipeline 20, thanomin crude product is from thanomin treating tower T2(packing tower, tower diameter is Φ 25mm, the Stainless Steel Helices of in-built Φ 3*3 θ ring, bed stuffing height is 0.8m) middle part charging, thanomin treating tower T2 tower top is the azeotrope of bis cyclohexane and thanomin, azeotrope is discharged from pipeline 24, enter condenser H4, a condensed azeotrope part is back to azeotropy rectification column T1 middle part charging through pipeline 27, and another part is as the backflow of thanomin treating tower T2; The tower reactor of thanomin treating tower T2 is thanomin, goes out from tower bottom flow through pipeline 22, and a part enters reboiler H3 and is recycled into thanomin treating tower T2 circulating vaporization through pipeline 21 again, and another part is through pipeline 23 extraction.
Embodiment 1: the azeotrope of triethylene diamine and thanomin, entrainer enters azeotropy rectification column, overhead fraction is the azeotrope of entrainer and thanomin, tower reactor cut is triethylene diamine and azeotropic agent composition, this mixture is through cooling, after crystallization, separate out solid, it is 99.8% that the solid phase prod obtaining after filtration is triethylene diamine product purity, described entrainer is bis cyclohexane, in azeotrope, the mol ratio of thanomin and bis cyclohexane is 1:1.25, the working pressure 20kPa of azeotropy rectification column, tower top temperature is 122.4 DEG C, tower reactor temperature is 145.8 DEG C, reflux ratio is 1.5, the overhead fraction of azeotropy rectification column T1 enters and divides mutually device V1 to divide mutually, and upper strata is entrainer, is circulated to azeotropy rectification column T1, and lower floor is thanomin crude product, enters thanomin treating tower T2, and the working pressure that wherein divides mutually device V1 is normal pressure, and service temperature is 32 DEG C, the overhead fraction of thanomin treating tower T2 is the azeotrope of entrainer and thanomin, be circulated to azeotropy rectification column T1, the tower reactor cut of thanomin treating tower T2 is thanomin, the wherein working pressure 10kPa of thanomin treating tower, tower top temperature is 106.5 DEG C, tower reactor temperature is 109.7 DEG C, and reflux ratio is 2.Logistics parameter in embodiment 1 is in table 1, and main equipment parameters is in table 2.
Logistics parameter in table 1 embodiment 1
Main equipment parameters in table 2 embodiment 1
Embodiment 2: the azeotrope of triethylene diamine and thanomin, entrainer enters azeotropy rectification column T1, overhead fraction is the azeotrope of entrainer and thanomin, tower reactor cut is triethylene diamine and azeotropic agent composition, this mixture is through cooling, crystallization solid, the solid phase prod obtaining after filtration is triethylene diamine, purity is 99.8%, described entrainer is naphthane, in azeotrope, the mol ratio of thanomin and naphthane is 1:2.25, the working pressure 20kPa of azeotropy rectification column, tower top temperature is 113.5 DEG C, tower reactor temperature is 126.1 DEG C, reflux ratio is 1.5, the overhead fraction of azeotropy rectification column T1 enters and divides mutually device V1 to divide mutually, and upper strata is entrainer, is circulated to azeotropy rectification column, and lower floor is thanomin crude product, enters thanomin treating tower T2, and the working pressure that wherein divides mutually device V1 is normal pressure, 32 DEG C of service temperatures, the overhead fraction of thanomin treating tower T2 is the azeotrope of entrainer and thanomin, is circulated to azeotropy rectification column, and thanomin treating tower tower reactor cut is thanomin, the wherein working pressure 10kPa of thanomin treating tower, tower top temperature is 94.5 DEG C, and tower reactor temperature is 109.7 DEG C, and reflux ratio is 3.Logistics parameter in embodiment 2 is in table 3, and main equipment parameters is in table 4.
Logistics parameter in table 3 embodiment 2
Main equipment parameters in table 4 embodiment 2
Comparative example 1: the azeotrope of triethylene diamine and thanomin, entrainer enters azeotropy rectification column T1, overhead fraction is the azeotrope of entrainer and thanomin, tower reactor cut is triethylene diamine and azeotropic agent composition, this mixture is through cooling, crystallization solid, the solid phase prod obtaining is after filtration triethylene diamine product purity 99.8%, described entrainer is p-Xylol, in azeotrope, the mol ratio of thanomin and p-Xylol is 1:8.25, the working pressure 20kPa of azeotropy rectification column T1, tower top temperature is 84.9 DEG C, tower reactor temperature is 122.8 DEG C, reflux ratio is 1.5, the overhead fraction of azeotropy rectification column T1 enters and divides mutually device V1 to divide mutually, and upper strata is entrainer, is circulated to azeotropy rectification column T1, and lower floor is thanomin crude product, enters thanomin treating tower T2, and the working pressure that wherein divides mutually device V1 is normal pressure, 32 DEG C of service temperatures, the overhead fraction of thanomin treating tower T2 is the azeotrope of entrainer and thanomin, is circulated to azeotropy rectification column T1, and thanomin treating tower T2 tower reactor cut is thanomin, the wherein working pressure 10kPa of thanomin treating tower, tower top temperature is 80.3 DEG C, and tower reactor temperature is 109.7 DEG C, and reflux ratio is 0.5.Logistics parameter in comparative example 1 is in table 5, and main equipment parameters is in table 6.
Logistics parameter in table 5 comparative example 1
Main equipment parameters in table 6 comparative example 1
Claims (2)
1. a separation method for triethylene diamine and thanomin azeotrope, is characterized in that, the method is carried out according to following steps:
(1) by the azeotrope of triethylene diamine and thanomin, entrainer is sent into azeotropy rectification column (T1), overhead fraction is the azeotrope of entrainer and thanomin, tower reactor cut is triethylene diamine and azeotropic agent composition, this mixture is separated out solid through cooling post crystallization, the solid obtaining is after filtering triethylene diamine product, thanomin in azeotrope and the mol ratio of entrainer are 3:1～1:2, working pressure 5kPa～the 50kPa of azeotropy rectification column (T1), tower top temperature is 100 DEG C～130 DEG C, tower reactor temperature is 130 DEG C～160 DEG C, reflux ratio is 0.5～4,
(2) overhead fraction of azeotropy rectification column (T1) enters and divides mutually device (V1) to divide mutually, upper strata is entrainer, be circulated to azeotropy rectification column (T1), lower floor is thanomin crude product, enter thanomin treating tower (T2), the described working pressure that divides mutually device (V1) is normal pressure, 25 DEG C～60 DEG C of service temperatures;
(3) overhead fraction of thanomin treating tower (T2) is the azeotrope of entrainer and thanomin, be circulated to azeotropy rectification column (T1), the tower reactor cut of thanomin treating tower (T2) is thanomin, wherein the working pressure of thanomin treating tower (T2) is 5kPa～20kPa, tower top temperature is 90 DEG C～120 DEG C, tower reactor temperature is 100 DEG C～130 DEG C, and reflux ratio is 0.5～3;
Described entrainer is bis cyclohexane or naphthane.
2. the separation method of triethylene diamine as claimed in claim 1 and thanomin azeotrope, is characterized in that, the method is carried out according to following steps:
(1) azeotrope of triethylene diamine and thanomin, entrainer bis cyclohexane enters azeotropy rectification column (T1), overhead fraction is the azeotrope of entrainer bis cyclohexane and thanomin, tower reactor cut is the mixture of triethylene diamine and entrainer bis cyclohexane, this mixture is separated out solid through cooling post crystallization, the solid obtaining is after filtering triethylene diamine product, in azeotrope, the mol ratio of thanomin and entrainer bis cyclohexane is 1:1.25, the working pressure of azeotropy rectification column (T1) is 20kPa, tower top temperature is 122.4 DEG C, tower reactor temperature is 145.8 DEG C, reflux ratio is 1.5,
(2) overhead fraction of azeotropy rectification column (T1) enters and divides mutually device (V1) to divide mutually, upper strata is entrainer bis cyclohexane, be circulated to azeotropy rectification column (T1), lower floor is thanomin crude product, enter thanomin treating tower (T2), the working pressure that wherein divides mutually device (V1) is normal pressure, 32 DEG C of service temperatures;
(3) overhead fraction of thanomin treating tower (T2) is the azeotrope of entrainer bis cyclohexane and thanomin, be circulated to azeotropy rectification column (T1), the tower reactor cut of thanomin treating tower (T2) is thanomin, the wherein working pressure 10kPa of thanomin treating tower (T2), tower top temperature is 106.5 DEG C, tower reactor temperature is 109.7 DEG C, and reflux ratio is 2.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210476478.2A CN103012412B (en) | 2012-11-21 | 2012-11-21 | Separation method of triethylene diamine and ethanolamine azeotrope |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210476478.2A CN103012412B (en) | 2012-11-21 | 2012-11-21 | Separation method of triethylene diamine and ethanolamine azeotrope |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103012412A CN103012412A (en) | 2013-04-03 |
| CN103012412B true CN103012412B (en) | 2014-08-27 |
Family
ID=47961564
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210476478.2A Active CN103012412B (en) | 2012-11-21 | 2012-11-21 | Separation method of triethylene diamine and ethanolamine azeotrope |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103012412B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104230941B (en) * | 2013-06-17 | 2016-08-10 | 中国石油化工股份有限公司 | The production method of triethylene diamine |
| CN103664964B (en) * | 2013-12-18 | 2016-03-02 | 西安近代化学研究所 | The absorption process of triethylene diamine production rectifying gas and device |
| CN105585508B (en) * | 2014-10-24 | 2017-10-27 | 中国石油化工股份有限公司 | The separation method of monoethanolamine and triethylene diamine crystalline hydrate |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3128275A (en) * | 1962-06-07 | 1964-04-07 | Jefferson Chem Co Inc | Method for the purification of triethylenediamine |
| US20020156278A1 (en) * | 2001-01-10 | 2002-10-24 | Ortmund Lang | Process for the preparation of pure triethylenediamine (TEDA) |
| CN102030755A (en) * | 2010-11-24 | 2011-04-27 | 西安近代化学研究所 | Method for preparing high-purity triethylene diamine |
| CN102584833A (en) * | 2011-12-20 | 2012-07-18 | 西安近代化学研究所 | Separation method for mixture of triethylene-diamine and ethanolamine |
| CN102584834A (en) * | 2011-12-20 | 2012-07-18 | 西安近代化学研究所 | Separation method for mixture of triethylene-diamine and ethanolamine |
-
2012
- 2012-11-21 CN CN201210476478.2A patent/CN103012412B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3128275A (en) * | 1962-06-07 | 1964-04-07 | Jefferson Chem Co Inc | Method for the purification of triethylenediamine |
| US20020156278A1 (en) * | 2001-01-10 | 2002-10-24 | Ortmund Lang | Process for the preparation of pure triethylenediamine (TEDA) |
| CN102030755A (en) * | 2010-11-24 | 2011-04-27 | 西安近代化学研究所 | Method for preparing high-purity triethylene diamine |
| CN102584833A (en) * | 2011-12-20 | 2012-07-18 | 西安近代化学研究所 | Separation method for mixture of triethylene-diamine and ethanolamine |
| CN102584834A (en) * | 2011-12-20 | 2012-07-18 | 西安近代化学研究所 | Separation method for mixture of triethylene-diamine and ethanolamine |
Non-Patent Citations (4)
| Title |
|---|
| 三乙烯二胺分离过程的模拟;金彦 等;《石油化工高等学校学报》;20060625;第19卷(第2期);第34-37页 * |
| 乙醇胺合成三乙烯二胺工艺的研究;尚会建 等;《聚氨酯工业》;20120428;第27卷(第2期);第23-26页 * |
| 尚会建 等.乙醇胺合成三乙烯二胺工艺的研究.《聚氨酯工业》.2012,第27卷(第2期),第23-26页. |
| 金彦 等.三乙烯二胺分离过程的模拟.《石油化工高等学校学报》.2006,第19卷(第2期),第34-37页. |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103012412A (en) | 2013-04-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105503492B (en) | A kind of MTP devices and its new separating technology | |
| CN102690172A (en) | Method for producing isopropanol by acetone hydrogenation | |
| CN109206291A (en) | A kind of separation method of chloromethanes-dimethyl ether | |
| CN103254030B (en) | The recovery method of by-product raffinate in coal-ethylene glycol production process | |
| TWI730093B (en) | Integrated process for making propene and propene oxide from propane | |
| CN103012412B (en) | Separation method of triethylene diamine and ethanolamine azeotrope | |
| RU2015130732A (en) | METHOD FOR ISOLATING ETHYLENE | |
| JP6681676B2 (en) | Method and apparatus for the cyclic treatment and purification of propylene | |
| CN102584834A (en) | Separation method for mixture of triethylene-diamine and ethanolamine | |
| CN101830788A (en) | Method for separating azeotropic mixture of ethyl methyl ketone and water through variable-pressure rectification | |
| JP2021500381A (en) | Method for producing ethyleneamine | |
| CN102584833B (en) | Separation method for mixture of triethylene-diamine and ethanolamine | |
| CN106518675B (en) | The method for producing dimethyl oxalate and by-product dimethyl carbonate | |
| CN102126958B (en) | Device and method for preparing high purity m/p-nitrotoluene by coupling rectification and crystallization | |
| CN101481304B (en) | Process for preparing aminic acid by methyl formate hydrolysis | |
| CN105541555A (en) | Reactive rectification method and device for separating ethylene glycol, propylene glycol and butylene glycol | |
| CN104262177B (en) | A kind of separation purification method of thick diglycolamine | |
| CN104130095A (en) | Cis-decahydronaphthalene and trans-decahydronaphthalene separating method | |
| CN103965055B (en) | The synthetic method of Isopropylamine | |
| CN109336847A (en) | A kind of distillation system and its workflow recycling propylene oxide raffinate | |
| CN102977037B (en) | Separation method of pyrazine and ethylenediamine mixture | |
| CN203247212U (en) | Recovering device of by-product raffinate generated in production process of coal-based ethylene glycol | |
| CN105585502B (en) | The method that catalytic ammoniation method produces ethylenediamine | |
| CN212476585U (en) | Waste heat recovery system of rectifying unit in cyclohexanol production process | |
| CN101811928A (en) | Method for preparing isopropyl benzene |
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 |