CN101260066A - Method for producing fatty acid amide from cocoanut oil acidifying oil - Google Patents
Method for producing fatty acid amide from cocoanut oil acidifying oil Download PDFInfo
- Publication number
- CN101260066A CN101260066A CNA2008100275121A CN200810027512A CN101260066A CN 101260066 A CN101260066 A CN 101260066A CN A2008100275121 A CNA2008100275121 A CN A2008100275121A CN 200810027512 A CN200810027512 A CN 200810027512A CN 101260066 A CN101260066 A CN 101260066A
- Authority
- CN
- China
- Prior art keywords
- fatty acid
- acid amide
- coconut oil
- oil
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method using sulfated coconut oil to produce fatty acid amide. Sulfated coconut oil is taken as the initial raw material, and is orderly polymerized, made a dehydrocarbon and ester exchange, distilled and amidated to produce fatty acid amide, wherein, at first, the sulfated coconut oil is added with polymerizing agent to react to cause the molecular weight of the sulfated coconut oil to be increased and the boiling point to rise in times; then the sulfated coconut oil polymer is evaporated to separate, then is added with methanol and catalyst to make an esterification reaction to generate coconut oil methyl ester; the coconut oil methyl ester is distilled and purified, and then is reacted with diethanolamine under normal pressure, and the fatty acid amide and the methanol can be obtained. The method uses the leftover produced by the refined coconut oil to produce the fatty acid amide, realizes the full utilization of the renewable resource, reduces the environmental pollution, can produce the fatty acid amide which is used for high-grade fine chemical industry products and has the quality exceeding the fatty acid amide produced with the refined coconut oil as the raw material, ensures that the cost of the fatty acid amide is greatly decreased, and has higher economic value.
Description
Technical field
The present invention relates to the fine chemistry industry production technique, particularly a kind of tankage that produce in the Oleum Cocois refining process that utilize, the processing method of producing the fatty acid amide that is used for detergent applications.
Background technology
The existing method that is used to produce fatty acid amide, mainly comprise the technology that adopts single stage method and two-step approach, these two kinds of processing methodes all must use the refining Oleum Cocois to be raw material, at present, the price of refining Oleum Cocois rises steadily on the market, makes to utilize the refining Oleum Cocois to produce the cost of fatty acid amide also constantly soaring.Like this, the tankage that produce in the development and use refining Oleum Cocois process are produced fatty acid amide and are not only had higher economic value, simultaneously also can the recycle and reuse waste, reduce environmental pollution, and meet the policy of national sustainable development.
Summary of the invention
At the deficiency of above existing fatty acid amide production technique, the purpose of this invention is to provide a kind of tankage that produce in the Oleum Cocois refining process that utilize, produce the processing method of fatty acid amide.
The objective of the invention is by realizing by the following technical solutions:
With the method that the cocinic acid carburetion is produced fatty acid amide, be starting raw material with the cocinic acid carburetion, produce fatty acid amide through following step successively, this method comprises:
(1) polymerization: the cocinic acid carburetion is added polymerizing agent, and temperature is controlled between 180 ℃-250 ℃, produces polyreaction, and its molecular weight is increased, and boiling point rises.
(2) take off hydrocarbon: utilize the acidifying oil polymer different, adopt method of evaporating to separate, can obtain the higher acidifying oil polymer of purity with paraffin boiling points.
(3) transesterify: the acidifying oil polymer that step (2) is obtained adds methyl alcohol and catalyzer, carries out the successive esterification, can generate coconut oil methyl ester, glycerine and polymerizing agent.
(4) distillation: the coconut oil methyl ester mixture that step (3) is obtained adopts distil process to purify, and can obtain quality and color and luster methyl esters preferably.
(5) amidation: higher coconut oil methyl ester and the diethanolamine of purity that step (4) is obtained reacts under normal pressure, can obtain fatty acid amide and methyl alcohol.
As the preferred technical solution of the present invention, the temperature that described step (1) adopts evaporation to separate the acidifying oil polymer is 200 ℃, and pressure is-6kpa.
As the preferred technical solution of the present invention, the temperature that described step (2) adopts evaporation to separate the acidifying oil polymer is 180 ℃ to 250 ℃, and pressure is-2kpa.
As the preferred technical solution of the present invention, the esterification reaction temperature of described step (3) is controlled at 50 ℃ to 70 ℃, and pressure is to carry out successive reaction under normal pressure.
As the preferred technical solution of the present invention, described step (4) distillatory temperature is controlled at 170 ℃ to 220 ℃, and pressure is-2kpa.
As the preferred technical solution of the present invention, the temperature of described step (5) amidate action is controlled between 10 ℃ to 150 ℃, and the reaction times is 6 to 8 hours.
The invention has the beneficial effects as follows:
The tankage that produce in the refining Oleum Cocois process that development and use went out of use in the past, not only can realize making full use of of renewable resource, reduce environmental pollution, can also produce the fatty acid amide that can be used for high-grade fine chemical product, it is the fatty acid amide of raw material production that its quality surpasses with the refining Oleum Cocois, the present invention reduces the production cost of fatty acid amide greatly, has higher economic value, also can reclaim simultaneously, the recycle waste.
Embodiment
Produce the method for fatty acid amide with the cocinic acid carburetion, the raw material that adopts is the tankage that produce in the Oleum Cocois refining process, it contains the impurity of 10%-15%, if directly use, quality product does not reach requirement, must purify earlier, amidation again, its method steps of specifically producing fatty acid amide comprises:
(1) polymerization workshop section: the cocinic acid carburetion is added polymerizing agent, temperature is controlled at 220 ℃, pressure is-6kpa, cocinic acid carburetion and polymerizing agent produce polyreaction, its molecular weight is increased, boiling point rises at double, has widened the gap with acidifying well cuts boiling point, makes to adopt physical purification to become possibility.
(2) take off hydrocarbon workshop section: utilize the acidifying oil polymer different with paraffin boiling points, adopt method of evaporating to separate, separation temperature is 200 ℃, separating pressure is-and carries out under the residual voltage of 2kpa, can obtain the higher acidifying oil polymer of purity.
(3) transesterify workshop section: the acidifying oil polymer that step (2) is obtained adds methyl alcohol and catalyzer, and 60 ℃ of temperature are carried out the successive esterification under the normal pressure, can generate coconut oil methyl ester, glycerine and polymerizing agent.
(4) distillation workshop section: the coconut oil methyl ester mixture that step (3) is obtained adopts distil process to purify, and distillation temperature is controlled at 200 ℃, and pressure is-2kpa, can obtain that purity is higher, quality and color and luster methyl esters preferably all.
(5) amidation workshop section: higher coconut oil methyl ester and the diethanolamine of purity that step (4) is obtained reacts under normal pressure, and temperature of reaction is controlled at 120 ℃, and the reaction times is 6 to 8 hours, can obtain the finished product of fatty acid amide and methyl alcohol.
Claims (6)
1, produce the method for fatty acid amide with the cocinic acid carburetion, it is characterized in that: with the cocinic acid carburetion is starting raw material, produces fatty acid amide through following step successively, and this method comprises:
(1) polymerization: the cocinic acid carburetion is added polymerizing agent, and temperature is controlled between 180 ℃-250 ℃, produces polyreaction, and its molecular weight is increased, and boiling point rises.
(2) take off hydrocarbon: utilize the acidifying oil polymer different, adopt method of evaporating to separate, can obtain the higher acidifying oil polymer of purity with paraffin boiling points.
(3) transesterify: the acidifying oil polymer that step (2) is obtained adds methyl alcohol and catalyzer, carries out the successive esterification, can generate coconut oil methyl ester, glycerine and polymerizing agent.
(4) distillation: the coconut oil methyl ester mixture that step (3) is obtained adopts distil process to purify, and can obtain that purity is higher, quality and color and luster methyl esters preferably.
(5) amidation: higher coconut oil methyl ester and the diethanolamine of purity that step (4) is obtained reacts under normal pressure, can obtain fatty acid amide and methyl alcohol.
2, method of producing fatty acid amide with the Oleum Cocois esterised oil according to claim 1, it is characterized in that: the temperature that described step (1) adopts evaporation to separate the acidifying oil polymer is 200 ℃, and pressure is-6kpa.
3, method of producing fatty acid amide with the Oleum Cocois esterised oil according to claim 1, it is characterized in that: the temperature that described step (2) adopts evaporation to separate the acidifying oil polymer is 180 ℃ to 250 ℃, and pressure is-2kpa.
4, method of producing fatty acid amide according to claim 1 with the Oleum Cocois esterised oil, it is characterized in that: the esterification reaction temperature of described step (3) is controlled at 50 ℃ to 70 ℃, and pressure is to carry out successive reaction under normal pressure.
5, method of producing fatty acid amide with the Oleum Cocois esterised oil according to claim 1, it is characterized in that: described step (4) distillatory temperature is controlled at 170 ℃ to 220 ℃, and pressure is-2kpa.
6, method of producing fatty acid amide according to claim 1 with the Oleum Cocois esterised oil, it is characterized in that: the temperature of described step (5) amidate action is controlled between 10 ℃ to 150 ℃, and the reaction times is 6 to 8 hours.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100275121A CN101260066B (en) | 2008-04-18 | 2008-04-18 | Method for producing fatty acid amide from cocoanut oil acidifying oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100275121A CN101260066B (en) | 2008-04-18 | 2008-04-18 | Method for producing fatty acid amide from cocoanut oil acidifying oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101260066A true CN101260066A (en) | 2008-09-10 |
| CN101260066B CN101260066B (en) | 2012-03-14 |
Family
ID=39960800
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008100275121A Expired - Fee Related CN101260066B (en) | 2008-04-18 | 2008-04-18 | Method for producing fatty acid amide from cocoanut oil acidifying oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101260066B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102240607A (en) * | 2011-04-13 | 2011-11-16 | 岳阳百丽工业油脂有限公司 | Oleamide sodium type phosphorite floatation agent and preparation method thereof |
| RU2635544C1 (en) * | 2017-02-03 | 2017-11-14 | Александр Владимирович Покровский | Emulsifier of reverse water-fuel emulsions |
| US20200377784A1 (en) * | 2019-05-28 | 2020-12-03 | Clariant International, Ltd. | Method For Inhibiting Gas Hydrate Blockage In Oil And Gas Pipelines |
| US11753576B2 (en) | 2019-05-28 | 2023-09-12 | Clariant International Ltd. | Method for inhibiting gas hydrate blockage in oil and gas pipelines |
-
2008
- 2008-04-18 CN CN2008100275121A patent/CN101260066B/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102240607A (en) * | 2011-04-13 | 2011-11-16 | 岳阳百丽工业油脂有限公司 | Oleamide sodium type phosphorite floatation agent and preparation method thereof |
| RU2635544C1 (en) * | 2017-02-03 | 2017-11-14 | Александр Владимирович Покровский | Emulsifier of reverse water-fuel emulsions |
| US20200377784A1 (en) * | 2019-05-28 | 2020-12-03 | Clariant International, Ltd. | Method For Inhibiting Gas Hydrate Blockage In Oil And Gas Pipelines |
| US11753576B2 (en) | 2019-05-28 | 2023-09-12 | Clariant International Ltd. | Method for inhibiting gas hydrate blockage in oil and gas pipelines |
| US11753577B2 (en) * | 2019-05-28 | 2023-09-12 | Clariant International Ltd. | Method for inhibiting gas hydrate blockage in oil and gas pipelines |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101260066B (en) | 2012-03-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101099127B1 (en) | Method of preparing of 60% or more cis-di(C4-C20)alkyl cyclohexane-1,4-dicarboxylate | |
| CN104086417B (en) | A kind of esterification process of tetramethylolmethane | |
| SG140551A1 (en) | Production of biodiesel and glycerin from high free fatty acid feedstocks | |
| CN101260066B (en) | Method for producing fatty acid amide from cocoanut oil acidifying oil | |
| CN101195572A (en) | Method for synthesizing fatty acid methyl ester | |
| CN103044197A (en) | Technological method for purifying1,4-butanediol and co-producing gamma-butyrolactone | |
| CN109721471B (en) | Method for purifying glycerin from by-product of biodiesel production | |
| CN101215233A (en) | Technique for producing fatty acid methyl ester | |
| WO2012119520A1 (en) | Method for preparing plasticizer with cta residue | |
| CN1915948A (en) | Method for refining glycerol being as byproduct of biology diesel oil | |
| CN103937617A (en) | Method for preparing EPA (Eicosapentaenoic Acid) and/or DHA (docosahexoenoic acid)-rich ethyl ester by using deacidification byproduct as raw material | |
| CN103848739A (en) | Production method of high-purity dimethyl fumarate | |
| CN105085253A (en) | Preparation technique of long-chain alcohol (methyl)acrylate | |
| JP2017521422A (en) | New lactic acid recovery method | |
| CN101775326B (en) | Synthesis method of ester oil | |
| CN103435487A (en) | Preparation method of phthalic acid esters | |
| CN101260064B (en) | Technique for producing N.N-ethylene bisoleamide | |
| CN113480401A (en) | Synthesis method of chloro-n-pentane | |
| JP2014514276A (en) | Method for converting glycerin to propylene glycol | |
| CN102627561A (en) | Preparation process for plasticizer-tributyl citrate | |
| CN101016473B (en) | Method of producing biological fuel oil from poor oil | |
| CN114713249B (en) | Catalyst for preparing dimer acid and trimer acid and application method thereof | |
| CN103524544A (en) | Production method of boric acid ester by repeatedly using and purifying waste liquid | |
| US10954182B2 (en) | Reactive distillation process/equipment for fatty acid ester hydrolysis to produce carboxylic acid and alcohol | |
| RU2814847C1 (en) | Method of processing glycerine-containing wastes |
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 | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180514 Address after: 529143 Mei Dachong, Mu Zhou Town, Xinhui District, Jiangmen, Guangdong Patentee after: Jiangmen Xinhui District garno Chang Oil Co., Ltd. Address before: 529000 D2 Middle East Village Industrial Zone, Jiangmen, Guangdong Patentee before: Jiangmen Jianghai Canola Chemical Development Co. Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120314 Termination date: 20200418 |