CN1250517C - Process for synthesizing iso octyl amine - Google Patents
Process for synthesizing iso octyl amine Download PDFInfo
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- CN1250517C CN1250517C CN 200310122670 CN200310122670A CN1250517C CN 1250517 C CN1250517 C CN 1250517C CN 200310122670 CN200310122670 CN 200310122670 CN 200310122670 A CN200310122670 A CN 200310122670A CN 1250517 C CN1250517 C CN 1250517C
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- Prior art keywords
- alcohol
- diatomite
- ammonia
- catalyzer
- hydrogen
- 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.)
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- 238000000034 method Methods 0.000 title claims abstract description 16
- LPULCTXGGDJCTO-UHFFFAOYSA-N 6-methylheptan-1-amine Chemical compound CC(C)CCCCCN LPULCTXGGDJCTO-UHFFFAOYSA-N 0.000 title abstract 3
- 230000002194 synthesizing effect Effects 0.000 title abstract 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 21
- 239000001257 hydrogen Substances 0.000 claims abstract description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 18
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 17
- BWDBEAQIHAEVLV-UHFFFAOYSA-N 6-methylheptan-1-ol Chemical compound CC(C)CCCCCO BWDBEAQIHAEVLV-UHFFFAOYSA-N 0.000 claims abstract description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 239000003054 catalyst Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims abstract description 11
- 239000002994 raw material Substances 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 238000009833 condensation Methods 0.000 claims abstract description 5
- 230000005494 condensation Effects 0.000 claims abstract description 5
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims abstract description 5
- 229910017816 Cu—Co Inorganic materials 0.000 claims description 13
- QNIVIMYXGGFTAK-UHFFFAOYSA-N octodrine Chemical compound CC(C)CCCC(C)N QNIVIMYXGGFTAK-UHFFFAOYSA-N 0.000 claims description 13
- 229960001465 octodrine Drugs 0.000 claims description 13
- 238000010189 synthetic method Methods 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000012808 vapor phase Substances 0.000 abstract description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract 2
- 229910052593 corundum Inorganic materials 0.000 abstract 2
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 2
- 230000009466 transformation Effects 0.000 description 7
- LTHNHFOGQMKPOV-UHFFFAOYSA-N 2-ethylhexan-1-amine Chemical compound CCCCC(CC)CN LTHNHFOGQMKPOV-UHFFFAOYSA-N 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 4
- YIWUKEYIRIRTPP-UHFFFAOYSA-N 2-ethylhexan-1-ol Chemical compound CCCCC(CC)CO YIWUKEYIRIRTPP-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000004587 chromatography analysis Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 239000012747 synergistic agent Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000006424 Flood reaction Methods 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003995 emulsifying agent Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000008396 flotation agent Substances 0.000 description 1
- 230000000749 insecticidal effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 239000006273 synthetic pesticide Substances 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a method for synthesizing isooctyl amine, isooctyl alcohol is used as raw materials, Cu, Co/AL2O3 and diatomite are used as a catalyst, wherein the catalyst of Cu, Co/AL2O3 and diatomite has the following components: 1.0 to 30.0% of Cu, 1.0% to 50.0% of Co, 0.005% to 0.3% of Ru, 0.1% to 0.7% of Mg, 0.1% to 5.0 % of Cr, and the mixture of the Al2O3 and the diatomite or either of the Al2O3 and the diatomite as the rest. The reaction is carried out in a vapor phase, a continuous type process is adopted, the operating condition of a pressure is a normal pressure to 4.0MPa, the temperature is 50 to 350 DEG C, the alcohol liquid airspeed is 0.3 to 1.5h<-1>, the molar ratio of ammonia to alcohol is 3.0 to 15.0, the molar ratio of hydrogen to alcohol is 1.0 to 10.0, and the catalyst use level is 0.25 to 2.0m<3> of alcohol /(hr. m<3>of the catalyst). The isooctyl alcohol is driven into a preheater and mixed and preheated with free ammonia and inflammable air, and then reacts in a reaction vessel, the materials after reaction are processed by condensation, cooling and gas-liquid separation, and the isooctyl amine is adopted as the product. The present invention has the advantages of simple process flow, high conversion rate, good selectivity, little outgrowth, concise separation flow, low power consumption and raw material consumption, and low production cost of the product.
Description
Technical field
The present invention relates to a kind of chemical synthesis process, especially a kind of is the synthetic method of the octodrine of raw material with the isooctyl alcohol.
Background technology
Octodrine (another name: 2 ethyl hexylamine) be a kind of organic synthesis intermediate with extensive use, be main raw material (synergistic agent and the agricultural chemicals mixing usefulness of synthetic pesticide synergistic agent, can improve insecticidal effect, reduce environmental pollution), also can be used as simultaneously synthetic dyestuff, pigment, tensio-active agent, sterilant intermediate, and the raw material of producing stablizer, sanitas, vulcanization accelerator, antioxidant, flotation agent, emulsifying agent.Existing synthetic method, transformation efficiency is low, poor selectivity, the flow process complexity, production cost is higher.
Summary of the invention
The present invention will solve above-mentioned described deficiency, and a kind of transformation efficiency height is provided, and selectivity is good, and by product is few, and flow process is simple, and production cost is low, is fit to the synthetic method of industrial octodrine.
The technical solution adopted for the present invention to solve the technical problems.The synthetic method of this octodrine is a raw material with the isooctyl alcohol, with Cu-Co/Al
2O
3-diatomite is catalyzer; Cu-Co/Al wherein
2O
3Consisting of of-diatomite catalyzer: Cu is 1.0～30.0%, and Co is 1.0～50.0%, and Ru is 0.005～0.3%, and Mg is 0.01～0.7%, and Cr is 0.1～5.0%, and all the other are Al
2O
3With one of diatomaceous mixture or both.This is reflected at gas phase and carries out, and adopts the continous way process, and its concrete operations condition is pressure: normal pressure～4.0Mpa, temperature: 50～350 ℃, and pure liquid hourly space velocity: 0.3～1.5h
-1, ammonia alcohol mol ratio: 3.0～15.0, hydrogen alcohol mol ratio: 1.0～10.0, catalyst levels: 0.25～2.0m
3Alcohol/(hrm
3Catalyzer).Isooctyl alcohol by volume pump squeeze into preheater and with ammonia, hydrogen mixing preheating after enter fixed-bed reactor reactions, reacting rear material is through condensation cooling, gas-liquid separation; Gas phase is utilized through the recycle compressor compression cycle, and liquid phase enters rectifying tower and separates purification: octodrine is as the product extraction; Ammonia, isooctyl alcohol turn back to feed system, and replenish a certain amount of hydrogen and ammonia, to keep the mol ratio of above-mentioned ammonia, hydrogen, isooctyl alcohol; Waste water purifies to the emission standard discharging.
Described Cu-Co/Al
2O
3Consisting of of-diatomite catalyzer: Cu is 2.0～20.0%, and Co is 2.0～40.0%, and Ru is 0.005～0.3%, and Mg is 0.01～0.7%, and Cr is 0.1～5.0%, and all the other are Al
2O
3With one of diatomaceous mixture or both.
Described operational condition is preferably: pressure: 0.1～2.0Mpa, and temperature: 150～280 ℃, pure liquid hourly space velocity: 0.6～1.2h
-1, ammonia alcohol mol ratio: 6.5～12.0, hydrogen alcohol mol ratio: 4.5～8.0, catalyst levels: 0.4～1.0m
3Alcohol/hrm
3Catalyzer.
The effect that the present invention is useful is: with isooctyl alcohol (another name 2-Ethylhexyl Alcohol) is the synthetic octodrine (another name 2 ethyl hexylamine) of raw material continuous catalysis ammonification dehydration.Present method technical process is simple, the transformation efficiency height, and selectivity is good, and by product is few, and separation process is simple and clear, and energy consumption, raw material consumption are low, and the products production cost is low.
Embodiment
Below in conjunction with embodiment the present invention is further described.
Embodiment 1: this octodrine (another name: 2 ethyl hexylamine, synthetic method C8H19N):
1) be raw material with the isooctyl alcohol,, with Cu-Co/Al
2O
3-diatomite is catalyzer; Cu-Co/Al wherein
2O
3-diatomite catalyzer is: with Al (OH)
3Be mixed with sodium aluminate solution with 46%NaOH, use the nitric acid neutralization precipitation, after overaging, filtration, washing, add a certain amount of diatomite and mix, through extrusion molding, drying, roasting, obtain diameter 4mm, the strip Al of length 3～7mm
2O
3-diatomite support is made mixing solutions with the nitrate of Cu, Co, Ru, Mg, Cr, in proportion to Al
2O
3-diatomite support floods, and puts into muffle furnace roasting 24h after the drying, makes content and be Cu4.5%, Co17.0%, Ru0.1%, Mg0.7%, Cr2.0%, all the other are Al
2O
3, the diatomite mixture Cu-Co/Al
2O
3-diatomite catalyzer.Catalyzer is numbered A-1.
2), this is reflected at gas phase and carries out, and adopts the continous way process, its concrete operations condition is pressure: 0.9Mpa, temperature: 200 ℃, pure liquid hourly space velocity: 0.3～1.0h
-1, ammonia alcohol mol ratio: 8.5, hydrogen alcohol mol ratio: 5.5, catalyst levels: 0.4～1.0m
3Alcohol/(hrm
3Catalyzer).
3), isooctyl alcohol by volume pump squeeze into preheater and with ammonia, hydrogen mixing preheating after enter fixed-bed reactor reactions, reacting rear material is through condensation cooling, gas-liquid separation; Gas phase is utilized through the recycle compressor compression cycle, and liquid phase enters rectifying tower and separates purification: octodrine is as the product extraction; Ammonia, isooctyl alcohol turn back to feed system, and replenish a certain amount of hydrogen and ammonia, to keep the mol ratio of above-mentioned ammonia, hydrogen, isooctyl alcohol; Waste water purifies to the emission standard discharging.
Embodiment 2: make according to embodiment 1 described method that content is Cu6.5%, Co17.0%, Ru0.1%, Mg0.7%, Cr2.0%, all the other are Al
2O
3, the diatomite mixture Cu-Co/Al
2O
3-diatomite catalyzer.Catalyzer is numbered A-2.
Embodiment 3: make according to embodiment 1 described method that content is Cu8.5%, Co17.0%, Ru0.1%, Mg0.7%, Cr2.0%, all the other are Al
2O
3, the diatomite mixture Cu-Co/Al
2O
3-diatomite catalyzer.Catalyzer is numbered A-3.
Embodiment 4: make according to embodiment 1 described method that content is Cu6.5%, Co18.5%, Ru0.1%, Mg0.7%, Cr2.0%, all the other are Al
2O
3, the diatomite mixture Cu-Co/Al
2O
3-diatomite catalyzer.Catalyzer is numbered A-4.
Embodiment 5: make according to embodiment 1 described method that content is Cu6.5%, Co20.0%, Ru0.1%, Mg0.7%, Cr2.0%, all the other are Al
2O
3, the diatomite mixture Cu-Co/Al
2O
3-diatomite catalyzer.Catalyzer is numbered A-5.
Embodiment 6---embodiment 11: with the catalyzer that is numbered A-4 among the embodiment 4 diameter of packing into is 32 * 3mm, the stainless steel reactor of length 1350mm.The stainless steel temperature-measuring casing of ∮ 8 * 1mm is set in the reactor, and catalyst packing height is 880mm, and loaded catalyst is 425ml.Reaction raw materials is to go out under enterprising, enters the separator after the condensation cooling from the effusive material of reactor bottom, and vapor phase ammonia, hydrogen are discharged the bottom liquid phases timing sampling from the separator top.Form concrete reaction conditions and the results are shown in table 1 with liquid-phase chromatographic analysis.
Table 1. reaction conditions and result
| The embodiment sequence number | The catalyzer numbering | Catalyzer Intake Quantity ml | Reaction conditions | Liquid product is formed, % | Transformation efficiency mol% | Selectivity mol% | |||||||
| Temperature ℃ | Pressure MP a | Air speed h -1 | Ammonia-alcohol ratio | Hydrogen alcohol ratio | 2-Ethylhexyl Alcohol | 2 ethyl hexylamine | By product | Water | |||||
| 1 | A-1 | 425 | 200 | 0.9 | 1.0 | 8.5 | 5.5 | 34.36 | 49.45 | 8.09 | 8.10 | 63.01 | 85.10 |
| 2 | A-2 | 425 | 215 | 0.9 | 1.0 | 8.5 | 5.5 | 30.36 | 54.34 | 6.72 | 8.58 | 67.13 | 88.31 |
| 3 | A-3 | 425 | 240 | 0.9 | 1.0 | 8.5 | 5.5 | 28.75 | 58.59 | 3.90 | 8.75 | 68.75 | 93.35 |
| 4 | A-4 | 425 | 250 | 0.9 | 1.0 | 8.5 | 5.5 | 25.78 | 59.65 | 5.44 | 9.13 | 71.91 | 91.11 |
| 6 | A-4 | 425 | 240 | 0.9 | 1.0 | 8.5 | 5.5 | 30.28 | 57.51 | 3.64 | 8.57 | 67.15 | 93.65 |
| 7 | A-4 | 425 | 240 | 1.0 | 1.0 | 8.5 | 5.5 | 29.17 | 57.38 | 4.73 | 8.71 | 68.32 | 91.89 |
| 8 | A-4 | 425 | 240 | 1.0 | 1.1 | 8.5 | 5.5 | 30.88 | 56.71 | 3.92 | 8.49 | 66.52 | 93.12 |
| 9 | A-4 | 425 | 240 | 1.0 | 1.0 | 9.0 | 5.5 | 26.90 | 60.90 | 2.82 | 8.97 | 70.67 | 95.31 |
| 10 | A-4 | 425 | 240 | 1.0 | 1.0 | 10.0 | 5.5 | 26.33 | 61.02 | 3.60 | 9.05 | 71.29 | 94.06 |
| 11 | A-4 | 425 | 240 | 1.0 | 1.0 | 9.0 | 6.5 | 27.10 | 60.98 | 2.96 | 8.96 | 70.46 | 95.05 |
| 5 | A-5 | 425 | 240 | 1.0 | 1.0 | 9.0 | 6.5 | 33.11 | 55.23 | 3.45 | 8.22 | 64.20 | 93.73 |
By data in the table 1 as can be known, react under present inventor's processing condition, the result all has higher transformation efficiency and selectivity preferably.
Embodiment 12: according to example 1～11 described device, flow process, filling 425ml A-4 catalyzer carries out 240 hours stable service tests.Reaction pressure: 1.0MPa, temperature: 240 ℃, pure liquid hourly space velocity: 1.0h
-1, ammonia alcohol mol ratio: 9.0, hydrogen alcohol mol ratio: 5.5.Form concrete reaction conditions and the results are shown in table 2 with liquid-phase chromatographic analysis.
Table 2.240 hour stable service test
| Accumulation h runtime | Liquid product is formed, w% | Transformation efficiency mol% | Selectivity mol% | |||
| 2-Ethylhexyl Alcohol | 2 ethyl hexylamine | By product | Water | |||
| 50 | 26.96 | 61.49 | 2.58 | 8.97 | 70.60 | 95.70 |
| 100 | 27.34 | 60.89 | 2.85 | 8.92 | 70.21 | 95.23 |
| 150 | 27.59 | 60.73 | 2.79 | 8.89 | 69.95 | 95.31 |
| 200 | 27.37 | 60.82 | 2.89 | 8.92 | 70.18 | 95.16 |
| 240 | 27.83 | 60.51 | 2.80 | 8.60 | 69.69 | 95.28 |
By table 2 data as can be known, under these processing condition, the transformation efficiency of reaction is higher than 70%, and selectivity is higher than 95%, and catalyzer has stability preferably simultaneously.
Claims (3)
1, a kind of synthetic method of octodrine is characterized in that:
1) be raw material with the isooctyl alcohol,, with Cu-Co/Al
2O
3-diatomite is catalyzer; Cu-Co/Al wherein
2O
3Consisting of of-diatomite catalyzer: Cu is 1.0～30.0%, and Co is 1.0～50.0%, and Ru is 0.005～0.3%, and Mg is 0.01～0.7%, and Cr is 0.1～5.0%, and all the other are Al
2O
3With one of diatomaceous mixture or both;
2), this is reflected at gas phase and carries out, and adopts the continous way process, its concrete operations condition is pressure: normal pressure～4.0Mpa, temperature: 50～350 ℃, pure liquid hourly space velocity: 0.3～1.5h
-1, ammonia alcohol mol ratio: 3.0～15.0, hydrogen alcohol mol ratio: 1.0～10.0, catalyst levels: 0.25～2.0m
3Alcohol/hrm
3Catalyzer;
3), isooctyl alcohol by volume pump squeeze into preheater and with ammonia, hydrogen mixing preheating after enter fixed-bed reactor reactions, reacting rear material is through condensation cooling, gas-liquid separation; Gas phase is utilized through the recycle compressor compression cycle, and liquid phase enters rectifying tower and separates purification: octodrine is as the product extraction; Ammonia, isooctyl alcohol turn back to feed system, and replenish a certain amount of hydrogen and ammonia, to keep the mol ratio of above-mentioned ammonia, hydrogen, isooctyl alcohol; Waste water purifies to the emission standard discharging.
2, the synthetic method of octodrine according to claim 1 is characterized in that: described Cu-Co/Al
2O
3Consisting of of-diatomite catalyzer: Cu is 2.0～20.0%, and Co is 2.0～40.0%, and Ru is 0.005～0.3%, and Mg is 0.01～0.7%, and Cr is 0.1～5.0%, and all the other are Al
2O
3With one of diatomaceous mixture or both.
3, the synthetic method of octodrine according to claim 1 is characterized in that: described operational condition is: pressure: 0.1～2.0Mpa, and temperature: 150～280 ℃, pure liquid hourly space velocity: 0.6～1.2h
-1, ammonia alcohol mol ratio: 6.5～12.0, hydrogen alcohol mol ratio: 4.5～8.0, catalyst levels: 0.4～1.0m
3Alcohol/hrm
3Catalyzer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310122670 CN1250517C (en) | 2003-12-24 | 2003-12-24 | Process for synthesizing iso octyl amine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310122670 CN1250517C (en) | 2003-12-24 | 2003-12-24 | Process for synthesizing iso octyl amine |
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|---|---|
| CN1554640A CN1554640A (en) | 2004-12-15 |
| CN1250517C true CN1250517C (en) | 2006-04-12 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018157395A1 (en) * | 2017-03-03 | 2018-09-07 | Rhodia Operations | Process for preparing an amine via a direct amination reaction |
| CN112547072B (en) * | 2019-09-10 | 2023-08-15 | 中国石油化工股份有限公司 | Supported catalyst and application and method for preparing lower aliphatic amine |
| CN114105780B (en) * | 2021-12-23 | 2024-02-02 | 潍坊加易加生物科技有限公司 | Synthesis method of isooctylamine and derivative by one-pot method |
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