CN100357024C - Catalyst for preparing fatty tertiary amine, prepn. method and application thereof - Google Patents
Catalyst for preparing fatty tertiary amine, prepn. method and application thereof Download PDFInfo
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- CN100357024C CN100357024C CNB2006100123100A CN200610012310A CN100357024C CN 100357024 C CN100357024 C CN 100357024C CN B2006100123100 A CNB2006100123100 A CN B2006100123100A CN 200610012310 A CN200610012310 A CN 200610012310A CN 100357024 C CN100357024 C CN 100357024C
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Abstract
The present invention relates to a catalyst for preparing aliphatic tertiary amine, which is composed of 20 to 40 wt% of a cupric oxide, 15 to 50 wt% of chromic oxide, 10 to 20 wt% of a third component and 0 to 30 wt% of a carrier. A coprecipitation method is used for preparing the catalyst which is used for the reaction for preparing tertiary amine by catalyzing aliphatic amide and adding hydrogen; the used amount of the catalyst is 1% to 20% of the weight of the aliphatic amide; the operational temperature is between 160 DEG C and 220 DEG C, the operational pressure is between 18 bars and 25 bars. The present invention has the advantages of low operational temperature, low operational pressure, high conversion rate of the aliphatic amide, high selectivity of products and easy operation.
Description
Technical field
The invention belongs to a kind of catalyst and method for making and application for preparing fat tertiary amine.
Background technology
Current home and overseas is produced the technology of tertiary amine mainly by the preparation of fatty alcohol one-step method.But the fatty alcohol price is higher, so this route cost is higher.Generate fatty acid amide by aliphatic acid and dimethylamine, catalytic hydrogenation prepares tertiary amine then, and this route raw fatty acid cost is low, and environmentally safe, belongs to environmental protection technology.The key that the acid amides catalytic hydrogenation prepares tertiary amine is choosing of catalyst.
Richard M.King, Cincinnati, Ohio be at U.S.Pat.No.4 in 1984, in 448,998, adopt composite catalyst (copper chromite is used zeolite as carrier), but the conversion ratio of acid amides is lower, and selection of catalysts is relatively poor.
Christian Forquy, Monein, L Isle Adam etc. be at U.S.Pat.No.5 in 1991, in 075,505, adopts the Cu-Cr-Mn catalyst series, obtains higher conversion ratio and selectivity.
U.S.Pat.No.4, in 448,998, the conversion ratio of acid amides is 91.6%, and selectivity 80.5%, reaction temperature are 287 ℃, and reaction pressure is 140bars.
U.S.Pat.No.5, in 075,505, the conversion ratio of acid amides reaches more than 99%, and selectivity reaches 88%, and reaction temperature is 235 ℃, and reaction pressure is 27bars.
Though the catalyst in these two pieces of patents can make fatty acid amide finish catalytic hydrogenation reaction effectively, needed reaction temperature and hypertonia are unfavorable for operation, and equipment requires high temperature high voltage resistant, equipment cost height.
Summary of the invention
The purpose of this invention is to provide a kind of reaction condition gentleness, the easy-operating method for preparing fat tertiary amine.
Catalyst component of the present invention comprises cupric oxide, chromium oxide, the 3rd component, carrier, and its percentage by weight consists of:
Cupric oxide 20～40%
Chromium oxide 15～50%
The 3rd component 10～20%
Carrier 0～30%
Preparation of catalysts method of the present invention mainly adopts coprecipitation,
Method for preparing catalyst one:
Form by catalyst weight percentage, with copper nitrate, the aqueous solution of chromic nitrate and the 3rd component metals nitrate or with copper nitrate, the aqueous solution of chromic nitrate and the 3rd component metals nitrate mixes with carrier, add thermal agitation, when temperature is 40-60 ℃, to dripping alkali liquid wherein, when pH reaches 6.0～7.5, stop to drip, be 65-100 ℃ in temperature and wore out 2-4 hour down, after leaving standstill 1-3 hour, with sediment filter, dry, at 300-500 ℃ of temperature lower calcination 3-5 hour, grind, sieve, obtain catalyst.
Preparation of catalysts method two of the present invention:
Form by catalyst weight percentage, earlier carrier is put into reactor in advance, and add that water is made into suspension or do not add carrier in reactor, only add entry, in temperature is under the 40-60 ℃ of condition, with copper nitrate, the aqueous solution of chromic nitrate and the 3rd component metals nitrate and alkali lye and stream add in the reactor, pH is between 6.0～7.5 in the control reactor, temperature be 65-100 ℃ aging 2-4 hour down, leave standstill 1-3 hour after, with sediment filter, dry, at 300-500 ℃ of temperature lower calcination 3-5 hour, grind, sieve, obtain catalyst.
Aforesaid the 3rd component is La
2O
3, CoO or NiO.
Aforesaid carrier is diatomite or 4A zeolite.
Aforesaid alkali lye is NaOH, potassium hydroxide or ammonia spirit.
Catalyst of the present invention is used for the reaction that the fatty acid amide catalytic hydrogenation prepares tertiary amine, and catalyst amount is generally 1～20% of fatty acid amide weight, is preferably 3～15%, operating temperature is 160～220 ℃, be preferably 180～200 ℃, operating pressure is 18～25bars, is preferably 20～23bars.
Aforesaid fatty acid amide is dodecyl dimethyl acid amides or myristyl dimethylformamide.
The present invention compared with prior art has following advantage:
Catalyst is used for the reaction that the fatty acid amide catalytic hydrogenation prepares tertiary amine, and operating temperature is low, and operating pressure is low, and the conversion ratio of fatty acid amide improves, and product selectivity is good, and synthetic route is brief, easy operating.
The specific embodiment
Embodiment 1
With 48.4gCu (NO
3)
23H
2O, 92.1gCr (NO
3)
39H
2O, 15.3gLa (NO
3)
36H
2O and 12.0g diatomite join in the distilled water of 1000mL, add thermal agitation, in the time of 40 ℃, begin to drip 1moL/LNaOH solution, when pH reaches 6.0, stop to drip, wore out two hours down for 65 ℃ in temperature, left standstill one hour, and, calcined 3h down at 300 ℃ with sediment filtration, drying, grind, sieve.Get the Cu-Cr-La composite catalyst.This catalyst fines contains cupric oxide 30.5wt%, chromium oxide 33.3wt%, lanthana 13.3wt%, diatomite 22.9wt%.
Above-mentioned catalyst 4.5g through behind the hydrogen reducing, is joined in the 150g dodecyl dimethyl acid amides, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 200 ℃, keep 30min under this temperature, then pressure is risen to 20bars, every 1h, the emptying gas reactor boosts to 20bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed by gas-chromatography, unreacted acid amides 0.4wt%, and dodecyl tertiary amine 88.8wt%, two dodecyl tertiary amine 5.0wt%, lauryl alcohol 4.3wt%, other high-boiling components content 1.5wt%. conversion ratio is 99.6%, selectivity is 89.2%
Embodiment 2
In advance with 51.4gCu (NO
3)
23H
2O, 43.2 gCr (NO
3)
39H
2O, 27.4gCo (NO
3)
26H
2O is heated to wiring solution-forming in the 1000mL distilled water, prepares 1moL/LKOH solution, 12.0g diatomite is joined in the distilled water of 300mL and is made into suspension, adds thermal agitation.When temperature reached 45 ℃, in the metallic solution and alkali lye and stream adding reactor that prepare in advance, control pH value was about 6.5 after dropwising.Wore out three hours down for 70 ℃ in temperature, left standstill two hours,, calcine 5h down, grind, sieve at 350 ℃ with sediment filtration, drying.Get the Cu-Cr-Co composite catalyst.This catalyst fines contains cupric oxide 38.5wt%, chromium oxide 18.6wt%, cobalt oxide 15.8wt%, diatomite 27.1wt%.
Above-mentioned catalyst 19.5g through behind the hydrogen reducing, is joined in the 127.5g myristyl dimethylformamide, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 200 ℃, keep 30min under this temperature, then pressure is risen to 23bars, every 1h, the emptying gas reactor boosts to 23bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.5wt%, myristyl tertiary amine 88.7wt%, two myristyl tertiary amine 4.8wt%, tetradecyl alchohol 4.7wt%, other high-boiling components content 1.3wt% by gas-chromatography.Conversion ratio is 99.5%, and selectivity is 89.1%
Embodiment 3
In advance with 23.2gCu (NO
3)
23H
2O, 76.8gCr (NO
3)
39H
2O, 7.0gLa (NO
3)
36H
2O is heated to wiring solution-forming in the 1000mL distilled water, prepares 1moL/L ammoniacal liquor, 6.0g 4A zeolite is joined in the distilled water of 300mL and is made into suspension, adds thermal agitation.When temperature reached 50 ℃, in the metallic solution and alkali lye and stream adding reactor that prepare in advance, control pH value was about 6.5 after dropwising.Wore out three hours down for 75 ℃ in temperature, left standstill two hours,, calcine 4h down, grind, sieve at 400 ℃ with sediment filtration, drying.Get the Cu-Cr-La composite catalyst.This catalyst fines contains cupric oxide 24.4wt%, chromium oxide 46.3wt%, lanthana 10.2wt%, 4A zeolite 19.1wt%.
Above-mentioned catalyst 7.5g through behind the hydrogen reducing, is joined in the 150g dodecyl dimethyl acid amides, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 190 ℃, keep 30min under this temperature, then pressure is risen to 22bars, every 1h, the emptying gas reactor boosts to 22bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.5wt%, dodecyl tertiary amine 88.3wt%, two dodecyl tertiary amine 4.2wt%, lauryl alcohol 6.0wt%, other high-boiling components content 1.0wt% by gas-chromatography.Conversion ratio is 99.5%, and selectivity is 88.7%
Embodiment 4
With 12.1gCu (NO
3)
23H
2O, 52.6gCr (NO
3)
39H
2O, 7.8g Co (NO
3)
26H
2O and 10.0g 4A zeolite join in the distilled water of 1000mL, add thermal agitation, in the time of 60 ℃, begin to drip 1moL/LNaOH solution, when pH reaches 7.0, stop to drip, wore out four hours down for 80 ℃ in temperature, left standstill three hours, and, calcined 5h down at 500 ℃ with sediment filtration, drying, grind, sieve.Get the Cu-Cr-Co composite catalyst.This catalyst fines contains cupric oxide 20wt%, chromium oxide 50wt%, cobalt oxide 10wt%, 4A zeolite 20wt%.
Above-mentioned catalyst 12.8g through behind the hydrogen reducing, is joined in the 127.5g myristyl dimethylformamide, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 180 ℃, keep 30min under this temperature, then pressure is risen to 20bars, every 1h, the emptying gas reactor boosts to 20bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.8wt%, myristyl tertiary amine 87.9wt%, two myristyl tertiary amine 4.0wt%, tetradecyl alchohol 5.1wt%, other high-boiling components content 2.2wt% by gas-chromatography.Conversion ratio is 99.2%, and selectivity is 88.6%
Embodiment 5
With 45.4gCu (NO
3)
23H
2O, 106.0gCr (NO
3)
39H
2O, 39.3gNi (NO
3)
26H
2O and 6.0g diatomite join in the distilled water of 1000mL, add thermal agitation, begin to drip 1moL/LKOH solution in the time of 55 ℃, when pH reaches 6.5, stop to drip, wore out two hours down for 100 ℃, left standstill one hour, sediment filtration, drying in temperature, calcine 4h down at 450 ℃, grind, sieve.Get the Cu-Cr-Ni composite catalyst.This catalyst fines contains cupric oxide 30.0wt%, chromium oxide 40.0wt%, nickel oxide 20.0wt%, diatomite 10.0wt%.
Above-mentioned catalyst 22.5g through behind the hydrogen reducing, is joined in the 150g dodecyl dimethyl acid amides, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 200 ℃, keep 30min under this temperature, then pressure is risen to 23bars, every 1h, the emptying gas reactor boosts to 23bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.6wt%, dodecyl tertiary amine 88.1wt%, two dodecyl tertiary amine 4.8wt%, lauryl alcohol 5.2wt%, other high-boiling components content 1.3wt% by gas-chromatography.Conversion ratio is 99.4%, and selectivity is 88.6%
Embodiment 6
With 60.5.4gCu (NO
3)
23H
2O, 106.0gCr (NO
3)
39H
2O, and 26.0gLa (NO
3)
36H
2O joins in the distilled water of 1000mL, adds thermal agitation, begins to drip 1moL/L ammoniacal liquor in the time of 50 ℃, when pH reaches 6.0, stop to drip, wore out two hours down for 60 ℃, left standstill two hours, sediment filtration, drying in temperature, calcine 3h down at 500 ℃, grind, sieve.Get the Cu-Cr-La composite catalyst.This catalyst fines contains cupric oxide 40.0wt%, chromium oxide 40.0wt%, and lanthana 20.0wt%,
Above-mentioned catalyst 6.5g through behind the hydrogen reducing, is joined in the 127.5g myristyl dimethylformamide, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 190 ℃, keep 30min under this temperature, then pressure is risen to 22bars, every 1h, the emptying gas reactor boosts to 22bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.7wt%, myristyl tertiary amine 87.5wt%, two myristyl tertiary amine 7.3wt%, tetradecyl alchohol 3.8wt%, other high-boiling components content 0.7wt% by gas-chromatography.Conversion ratio is 99.3%, and selectivity is 88.1%
Embodiment 7
Catalyst 15g in the foregoing description 1 is joined in the 150g dodecyl dimethyl acid amides, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 180 ℃, keep 30min under this temperature, then pressure is risen to 20bars, every 1h, the emptying gas reactor boosts to 20bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.7wt%, dodecyl tertiary amine 87.7wt%, two dodecyl tertiary amine 5.6wt%, lauryl alcohol 4.6wt%, other high-boiling components content 1.4wt% by gas-chromatography.Conversion ratio is 99.3%, and selectivity is 88.3%
Embodiment 8
Catalyst 4.5g in the foregoing description 2 is joined in the 127.5g myristyl dimethylformamide, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 200 ℃, keep 30min under this temperature, then pressure is risen to 20bars, every 1h, the emptying gas reactor boosts to 20bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.3wt%, myristyl tertiary amine 88.2wt%, two myristyl tertiary amine 5.0wt%, tetradecyl alchohol 5.0wt%, other high-boiling components content 1.5wt% by gas-chromatography.Conversion ratio is 99.7%, and selectivity is 88.5%
Embodiment 9
Catalyst 22.5g in the foregoing description 3 is joined in the 150g dodecyl dimethyl acid amides, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 200 ℃, keep 30min under this temperature, then pressure is risen to 23bars, every 1h, the emptying gas reactor boosts to 23bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.6wt%, dodecyl tertiary amine 87.6wt%, two dodecyl tertiary amine 5.4wt%, lauryl alcohol 5.4wt%, other high-boiling components content 1.0wt% by gas-chromatography.Conversion ratio is 99.4%, and selectivity is 88.1%
Embodiment 10
Catalyst 6.5g in the foregoing description 4 is joined in the 127.5g myristyl dimethylformamide, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 190 ℃, keep 30min under this temperature, then pressure is risen to 22bars, every 1h, the emptying gas reactor boosts to 22bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.7wt%, myristyl tertiary amine 87.9wt%, two myristyl tertiary amine 5.8wt%, tetradecyl alchohol 4.4wt%, other high-boiling components content 1.2wt% by gas-chromatography.Conversion ratio is 99.3%, and selectivity is 88.5%
Embodiment 11
Catalyst 4.5g in the foregoing description 5 is joined in the 150g dodecyl dimethyl acid amides, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 200 ℃, keep 30min under this temperature, then pressure is risen to 20bars, every 1h, the emptying gas reactor boosts to 20bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.8wt%, dodecyl tertiary amine 88.7wt%, two dodecyl tertiary amine 7.0wt%, lauryl alcohol 2.0wt%, other high-boiling components content 1.5wt% by gas-chromatography.Conversion ratio is 99.2%, and selectivity is 89.4%
Embodiment 12
Catalyst 12.8g in the foregoing description 6 is joined in the 127.5g myristyl dimethylformamide, drop in the 0.5L autoclave N while stirring
2Replace five times, heat up, stir, when temperature reaches 180 ℃, keep 30min under this temperature, then pressure is risen to 20bars, every 1h, the emptying gas reactor boosts to 20bars again, feeds dimethylamine gas in the reaction later stage, suppresses side reaction and takes place.The reaction end product is analyzed unreacted acid amides 0.9wt%, myristyl tertiary amine 87.6wt%, two myristyl tertiary amine 4.6wt%, tetradecyl alchohol 5.2wt%, other high-boiling components content 1.7wt% by gas-chromatography.Conversion ratio is 99.1%, and selectivity is 88.4%.
Claims (8)
1, a kind of catalyst for preparing fat tertiary amine is characterized in that the percentage by weight of catalyst component consists of:
Cupric oxide 20～40% chromium oxide 15～50%
The 3rd component 10～20% carriers 0～30%
Described the 3rd component is La
2O
3, CoO or NiO.
2, a kind of catalyst for preparing fat tertiary amine as claimed in claim 1 is characterized in that described carrier is diatomite or 4A zeolite.
3, a kind of Preparation of catalysts method for preparing fat tertiary amine as claimed in claim 1 or 2 is characterized in that comprising the steps:
Form by catalyst weight percentage, with copper nitrate, the aqueous solution of chromic nitrate and the 3rd component metals nitrate or with copper nitrate, the aqueous solution of chromic nitrate and the 3rd component metals nitrate mixes with carrier, add thermal agitation, when temperature is 40-60 ℃, to dripping alkali liquid wherein, when pH reaches 6.0～7.5, stop to drip, be 65-100 ℃ in temperature and wore out 2-4 hour down, after leaving standstill 1-3 hour, with sediment filter, dry, at 300-500 ℃ of temperature lower calcination 3-5 hour, grind, sieve, obtain catalyst.
4, a kind of Preparation of catalysts method for preparing fat tertiary amine as claimed in claim 1 or 2 is characterized in that comprising the steps:
Form by catalyst weight percentage, earlier carrier is put into reactor in advance, and add that water is made into suspension or do not add carrier in reactor, only add entry, in temperature is under the 40-60 ℃ of condition, with copper nitrate, the aqueous solution of chromic nitrate and the 3rd component metals nitrate and alkali lye and stream add in the reactor, pH is between 6.0～7.5 in the control reactor, temperature be 65-100 ℃ aging 2-4 hour down, leave standstill 1-3 hour after, with sediment filter, dry, at 300-500 ℃ of temperature lower calcination 3-5 hour, grind, sieve, obtain catalyst.
5, as claim 3 or 4 described a kind of Preparation of catalysts methods that prepare fat tertiary amine, it is characterized in that described alkali lye is NaOH, potassium hydroxide or ammonia spirit.
6, a kind of Application of Catalyst method for preparing fat tertiary amine as claimed in claim 1 or 2, it is characterized in that comprising the steps: that catalyst is used for the reaction that the fatty acid amide catalytic hydrogenation prepares tertiary amine, catalyst amount is 1～20% of a fatty acid amide weight, operating temperature is 160～220 ℃, and operating pressure is 18～25bars.
7, as each described a kind of Application of Catalyst method for preparing fat tertiary amine of claim 6, it is characterized in that described fatty acid amide is dodecyl dimethyl acid amides or myristyl dimethylformamide.
8, as each described a kind of Application of Catalyst method for preparing fat tertiary amine of claim 6, it is characterized in that catalyst amount is 3～15% of a fatty acid amide weight, operating temperature is 180～200 ℃, and operating pressure is 20～23bars.
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| CN100357024C true CN100357024C (en) | 2007-12-26 |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100435947C (en) * | 2006-12-20 | 2008-11-26 | 中国日用化学工业研究院 | Catalyst for preparing fatty primary amine by fatty nitrile hydrogenation and application thereof |
| CN103965053B (en) * | 2014-05-21 | 2015-07-01 | 华东理工大学 | Synthesis method of tertiary aliphatic amine |
| CN109126801A (en) * | 2018-08-28 | 2019-01-04 | 山东泰和水处理科技股份有限公司 | A kind of tertiary-aminated loaded catalyst of fatty alcohol and its preparation method and application |
| CN109046361A (en) * | 2018-08-28 | 2018-12-21 | 山东泰和水处理科技股份有限公司 | A kind of fatty alcohol TERTIARY AMINATING CATALYST and the preparation method and application thereof |
| CN110270279B (en) * | 2019-07-12 | 2021-10-08 | 江苏万盛大伟化学有限公司 | Fixed bed reactor for continuously producing diisotridecylamine and application thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4448998A (en) * | 1982-11-22 | 1984-05-15 | The Procter & Gamble Company | Catalytic hydrogenation of N,N-disubstituted amides to amines |
| US5025098A (en) * | 1989-09-08 | 1991-06-18 | Monsanto Company | Method of preparing bicyclic tetrahydroxylated pyrrolizidines |
| US5075505A (en) * | 1988-07-08 | 1991-12-24 | Ceca, S.A. | Process for obtaining n,n-dimethyl-n-alkylamines |
-
2006
- 2006-01-06 CN CNB2006100123100A patent/CN100357024C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4448998A (en) * | 1982-11-22 | 1984-05-15 | The Procter & Gamble Company | Catalytic hydrogenation of N,N-disubstituted amides to amines |
| US5075505A (en) * | 1988-07-08 | 1991-12-24 | Ceca, S.A. | Process for obtaining n,n-dimethyl-n-alkylamines |
| US5025098A (en) * | 1989-09-08 | 1991-06-18 | Monsanto Company | Method of preparing bicyclic tetrahydroxylated pyrrolizidines |
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Effective date of registration: 20090605 Address after: Room 118, 303 Ling Ling Road, Shanghai Waigaoqiao Free Trade Zone Patentee after: Run Fu Fu Chemical International Trading (Shanghai) Co., Ltd. Address before: No. 34, Wen Yuan alley, Taiyuan, Shanxi Patentee before: Chinese Daily Use Chemical Industry Research Inst. |
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| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Boxing China Resources Oleochemicals Co., Ltd. Assignor: Run Fu Fu Chemical International Trading (Shanghai) Co., Ltd. Contract fulfillment period: 2009.7.31 to 2016.7.30 contract change Contract record no.: 2009310000241 Denomination of invention: Catalyst for preparing fatty tertiary amine, prepn. method and application thereof Granted publication date: 20071226 License type: Exclusive license Record date: 2009.9.30 |
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| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.7.31 TO 2016.7.30; CHANGE OF CONTRACT Name of requester: BOXING HUARUN GREASE CHEMICAL CO., LTD. Effective date: 20090930 |
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| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20071226 Termination date: 20100208 |