CN104877761A - Process for extracting oleic acid from waste cooking oil - Google Patents
Process for extracting oleic acid from waste cooking oil Download PDFInfo
- Publication number
- CN104877761A CN104877761A CN201510302013.9A CN201510302013A CN104877761A CN 104877761 A CN104877761 A CN 104877761A CN 201510302013 A CN201510302013 A CN 201510302013A CN 104877761 A CN104877761 A CN 104877761A
- Authority
- CN
- China
- Prior art keywords
- oil
- reaction
- oleic acid
- waste
- acid
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/02—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/02—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils
- C11C1/025—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils by saponification and release of fatty acids
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/08—Refining
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention discloses a process for extracting oleic acid from waste cooking oil. The pretreatment and purification processes on waste oil are completed through eight steps including settling impurity removal, hydrated degumming, centrifugal separation, decolorizing reaction, dehydration reaction, saponification salting-out reaction, fatty acid refining and stearic acid and oleic acid extraction. The process has the advantage that pretreatment lays good foundation for purification, so that the separation effect reaches the optimum; the production cost is low, the process for effectively reusing wastes is developed, and the problems of waste grease backflow into cooking oil markets, environment pollution and resource waste are solved.
Description
Technical field
The present invention relates to a kind of complete processing of carrying out recycling treatment of food wastes, particularly a kind of technique extracting oleic acid from waste cooking oil.
Background technology
Waste edible oil from catering trade fishes for from the trench oil trap of hotel, restaurant.Its outward appearance is tawny, has off-odor, containing much harmful composition, is the waste oil that cannot eat.If do not recycled, not only waste valuable natural resources, also can cause secondary pollution.Therefore, the comprehensive utilization of waste oil has important practical significance, and it can be turned waste into wealth, turn harm into good.But source is unstable in waste oil, the a large amount of mechanical impurity contained and colloid, substantially increase the unsaponifiables number of components in waste grease and content, traditional oil refining process comprises bleaching earth adsorption method, alkali refining method and acid refining method etc., is difficult to effectively remove not saponification component.
Summary of the invention
The object of this invention is to provide and a kind of extract four extraction work steps by saltout reaction, lipid acid oelic acid and stearic acid of removing impurity by means of precipitation, hydration degum, centrifugation three pre-treatment work steps and decoloring reaction, dehydration reaction, saponification, extract the technique of stearic acid and oleic acid from waste cooking oil simultaneously, pre-treatment and extraction process combine, improve final oleic acid quality, solve the problem that waste grease backflow enters edible oil market and contaminate environment, the wasting of resources.
For achieving the above object, comprise the following steps,
(1) removing impurity by means of precipitation: waste oil is left standstill 7 ~ 10 hours, perforated lower floor residue precipitation;
(2) hydration degum: add water by the oil processed through step (1), amount of water is 1.2 ~ 1.8% of oil quality, then under the constant temperature of 70 ~ 80 DEG C, reaction 35 ~ 45min;
Preferably, amount of water is 1.5% of oil quality, and temperature of reaction is 75 DEG C, and the reaction times is 40min;
(3) centrifugation: the oil through step (2) is carried out centrifugation, rotating speed is 3500 ~ 4500r/min, centrifugal 10 ~ 25min;
(4) decoloring reaction: add atlapulgite and water glass by the oil of step (3), while stir general heating, Heating temperature is 75 ~ 95 DEG C, reaction 35 ~ 55min, the mass ratio of described atlapulgite and water glass is 3.5 ~ 4.5:1, always add that quality is oil quality 8.5% ~ 9.5%;
Preferably, atlapulgite and water glass mass ratio are 4:1, and total mass is 9%, and temperature of reaction is 85 DEG C, and the reaction times is 45min.
(5) dehydration reaction: first the oil through step (4) is squeezed into normal pressure dehydrating kettle, temperature is set to 125 DEG C;
(6) saponification is saltoutd reaction: the oil after step (5) dehydration adds 20% sodium hydroxide solution under normal pressure 100 DEG C of constant temperature stir, mass ratio 1:1.8 ~ 2.8 of sodium hydroxide solution and the oil after step (5) is dewatered, ethylene glycol or the alcohol of 20ml is added, until solution transforms is solid in every gram of waste oil; Add warm saturated aqueous common salt while hot while stirring to carry out saltouing, leaving standstill 2h, cooling, collects all white particles;
The feed postition of sodium hydroxide solution is preferably: dropwise add 1/3 of sodium hydroxide solution total amount during beginning, after reaction 1h, dropwise adds the half of remaining alkali lye, after reaction 1.5h, dropwise adds residue alkali lye;
(7) lipid acid is refined: be dissolved in water by the white particle that step (6) is formed, 90 ~ 100 DEG C of heated and stirred, and after dissolving completely, adjust ph is 8, and adds saturated acetic acid lead solution, produces and precipitates in a large number, leaves standstill cooled and filtered, retains precipitation;
(8) oleic acid and stearic acid extract: add the ethanol that concentration is 80% in the precipitation formed in step (7) a metallic, add-on is the ethanol adding 3g in every gram of oil, and heating in water bath dissolves, make the transparent brown color of solution, then cool, stearic acid is then separated out with crystal, and residue is oleic acid.Production cost of the present invention is low, develops the technique of a refuse reclamation effectively, solves the problem that waste grease backflow enters edible oil market and contaminate environment, the wasting of resources.
Positively effect of the present invention is as follows:
The present invention greatly reduces the difficulty of extraction by removing impurity by means of precipitation, hydration degum, centrifugation three pre-treatment work steps, reduce the mass content of phospholipids content, unsaponifiable matter content and esterification carbon distribution, improve the quality of subsequent extractions stearic acid and oleic acid stock oil, pre-treatment is that good basis has been established in purification.The present invention extracts eight steps by the saltout refining and oleic acid of reaction, lipid acid and stearic acid of removing impurity by means of precipitation, hydration degum, centrifugation, decoloring reaction, dehydration reaction, saponification, complete the process of pre-treatment to waste oil and purification, separating effect reaches best.Thus, develop the technique of a refuse reclamation effectively, solve the problem that waste grease backflow enters edible oil market and contaminate environment, the wasting of resources.
Embodiment
Further will describe in detail embodiments of the invention below.
A kind of technique extracting oleic acid from waste cooking oil of the present invention, its embodiment comprises the following steps:
Embodiment 1:
(1) removing impurity by means of precipitation: waste oil is left standstill 8 hours, perforated lower floor residue precipitation;
(2) hydration degum: because waste edible oil from catering trade is fried through multiple high temp, containing plurality of impurities, pollution substance, acid number is higher, so will remove phosphatide wherein.The waste oil processed through step (1) is added water, and the quality of water is 1.5% of the waste oil quality processed through step (1), and temperature of coming unstuck is 75 DEG C, reaction 40min;
(3) centrifugation: the waste oil processed through step (2) carries out centrifugation, rotating speed is 4000r/min, centrifugal 20min.
(4) decoloring reaction: add in the oil of step (3) for the atlapulgite of 9% of the quality of oil that processes through step (3) and the mixture of water glass by always adding quality, atlapulgite and water glass mass values are 4:1, while stir general heating, Heating temperature is 85 DEG C, reaction 45min.
Behind step (1) ~ (4), the mass percent that oily phospholipids content, unsaponifiable matter content and esterification carbon distribution account for oil quality is respectively 0.11%, 0.43% and 0.21%.
(5) dehydration reaction: first the grease through step (4) is squeezed into normal pressure dehydrating kettle, open fire in grease is removed, then the grease after normal pressure being dewatered, flash-evaporation dehydration still is drawn in by vacuum, hot steam is passed in flash-evaporation dehydration still heating jacket, heating jacket wall working temperature is 125 DEG C, and grease slides from flash-evaporation dehydration still top along heating jacket wall, and most of moisture content is sloughed.
(6) saponification is saltoutd reaction:
Oil after dehydration adds 20% sodium hydroxide solution under normal pressure 100 DEG C of constant temperature, sodium hydroxide and the waste oil mass ratio after dewatering are 1:2, ethylene glycol or the alcohol of 20ml is added in every gram of waste oil, to improve the boiling point of grease and to increase solubleness, controlling pH value is 9 ~ 10,1/3 of sodium hydroxide solution total amount is dropped into during beginning, after reaction 1h, dropwise add the half of remaining alkali lye, after reaction 1.5h, dropwise add residue alkali lye, add fashionable continuous stirring, in saponification process, moisture constantly evaporates, and needs suitable make up water.Can observe in reaction, during beginning, reaction mass forms emulsion, but carries out being converted into solid close to when completing in reaction.
After soap glue is formed, add while stirring while hot and turn the warm saturated aqueous common salt got ready in advance and carry out saltouing, leave standstill 2h, cooling, collects all white particles.The object of saltouing be salt adding after soap glue, the electric charge of soap glue and other impurity is neutralized, impels glue polymers to separate with water.
(7) lipid acid is refined: be dissolved in water by white particle, 90 ~ 100 DEG C of heated and stirred, and after dissolving completely, adjust ph is 8, and adds saturated acetic acid lead solution, produces and precipitates in a large number, leaves standstill cooled and filtered, retains precipitation.
(8) oleic acid and stearic acid extract: present industrial general employing methyl alcohol as extraction agent, although but the lower toxicity of methyl alcohol cost is larger.The present invention selects ethanol as extraction agent, and the concentration of ethanol is 80%, can reach the object be separated according to stearic acid with oleic acid different solubility in ethanol.Oleic acid solubleness is in ethanol much larger than stearic acid, and when adopting ethanol to extract stearic acid and oleic acid mixture, oleic acid is dissolved in liquid phase, and stearic acid is then separated out with crystal.Separated by filter operation, filter cake is then stearic acid, and liquid phase is through distillation process, and reclaim ethanol, residue is oleic acid.To add the industrial alcohol of 3g in every gram of oil, heating in water bath dissolves, and makes the transparent brown color of solution, then cool, then adularescent fish scale-like stearic acid crystallization, then carries out press filtration, and with appropriate cold washing with alcohol filter cake to pure white look, dry, obtain stearic acid.Namely filtrate obtain oleic acid product through Distillation recovery ethanol simultaneously.
The stearic saponification value of gained, acid number, moisture and mineral acid are respectively: 200 mgKOH/g, 215mgKOH/g, 0.21% and 0.0008%.
The saponification value of gained oleic acid, acid number, moisture and mineral acid are respectively: 199 mgKOH/g, 201 mgKOH/g, 0.18%, 0.0010%.
Embodiment 2
(1) removing impurity by means of precipitation: waste oil is left standstill 10 hours, perforated lower floor residue precipitation;
(2) hydration degum: because waste edible oil from catering trade is fried through multiple high temp, containing plurality of impurities, pollution substance, acid number is higher, so will remove phosphatide wherein.The waste oil processed through step (1) is added water, and the quality of water is 1.2% of the waste oil quality processed through step (1), and temperature of coming unstuck is 80 DEG C, reaction 35min;
(3) centrifugation: the waste oil processed through step (2) carries out centrifugation, rotating speed is 3500r/min, centrifugal 25min.
(4) decoloring reaction: add in the oil of step (3) for the atlapulgite of 9.5% of the quality of oil that processes through step (3) and the mixture of water glass by always adding quality, atlapulgite and water glass mass values are 3.5:1, while stir general heating, Heating temperature is 75 DEG C, reaction 55min.
The mass percent that the phospholipids content of the oil behind step (1) ~ (4), unsaponifiable matter content and esterification carbon distribution account for oil quality is respectively 0.15%, 0.48% and 0.18%.
(5) dehydration reaction: first the grease through step (4) is squeezed into normal pressure dehydrating kettle, open fire in grease is removed, then the grease after normal pressure being dewatered, flash-evaporation dehydration still is drawn in by vacuum, hot steam is passed in flash-evaporation dehydration still heating jacket, heating jacket wall working temperature is 125 DEG C, and grease slides from flash-evaporation dehydration still top along heating jacket wall, and most of moisture content is sloughed.
(6) saponification is saltoutd reaction:
Oil after dehydration adds 20% sodium hydroxide solution under normal pressure 100 DEG C of constant temperature, sodium hydroxide and the waste oil mass ratio after dewatering are 1:2.8, ethylene glycol or the alcohol of 20ml is added in every gram of waste oil, to improve the boiling point of grease and to increase solubleness, controlling pH value is 9 ~ 10,1/3 of sodium hydroxide solution total amount is dropped into during beginning, after reaction 1h, dropwise add the half of remaining alkali lye, after reaction 1.5h, dropwise add residue alkali lye, add fashionable continuous stirring, in saponification process, moisture constantly evaporates, and needs suitable make up water.Can observe in reaction, during beginning, reaction mass forms emulsion, but carries out being converted into solid close to when completing in reaction.
After soap glue is formed, add while stirring while hot and turn the warm saturated aqueous common salt got ready in advance and carry out saltouing, leave standstill 2h, cooling, collects all white particles.The object of saltouing be salt adding after soap glue, the electric charge of soap glue and other impurity is neutralized, impels glue polymers to separate with water.
(7) lipid acid is refined: be dissolved in water by white particle, 90 ~ 100 DEG C of heated and stirred, and after dissolving completely, adjust ph is 8, and adds saturated acetic acid lead solution, produces and precipitates in a large number, leaves standstill cooled and filtered, retains precipitation.
(8) stearic acid and oleic acid extract: present industrial general employing methyl alcohol as extraction agent, although but the lower toxicity of methyl alcohol cost is larger.The present invention selects ethanol as extraction agent, and the concentration of ethanol is 80%, can reach the object be separated according to stearic acid with oleic acid different solubility in ethanol.Oleic acid solubleness is in ethanol much larger than stearic acid, and when adopting ethanol to extract stearic acid and oleic acid mixture, oleic acid is dissolved in liquid phase, and stearic acid is then separated out with crystal.Separated by filter operation, filter cake is then stearic acid, and liquid phase is through distillation process, and reclaim ethanol, residue is oleic acid.To add the industrial alcohol of 3g in every gram of oil, heating in water bath dissolves, and makes the transparent brown color of solution, then cool, then adularescent fish scale-like stearic acid crystallization, then carries out press filtration, and with appropriate cold washing with alcohol filter cake to pure white look, dry, obtain stearic acid.Namely filtrate obtain oleic acid product through Distillation recovery ethanol simultaneously.
The stearic saponification value of gained, acid number, moisture and mineral acid are respectively: 208 mgKOH/g, 221mgKOH/g, 0.31% and 0.0015%.
The saponification value of gained oleic acid, acid number, moisture and mineral acid are respectively: 204mgKOH/g, 209mgKOH/g, 0.22%, 0.0013%.
Embodiment 3
(1) removing impurity by means of precipitation: waste oil is left standstill 7 hours, perforated lower floor residue precipitation;
(2) hydration degum: because waste edible oil from catering trade is fried through multiple high temp, containing plurality of impurities, pollution substance, acid number is higher, so will remove phosphatide wherein.The waste oil processed through step (1) is added water, and the quality of water is 1.8% of the waste oil quality processed through step (1), and temperature of coming unstuck is 70 DEG C, reaction 45min;
(3) centrifugation: the waste oil processed through step (2) carries out centrifugation, rotating speed is 4500r/min, centrifugal 10min.
(4) decoloring reaction: add in the oil of step (3) for the atlapulgite of 9.5% of the quality of oil that processes through step (3) and the mixture of water glass by always adding quality, atlapulgite and water glass mass values are 4.5:1, while stir general heating, Heating temperature is 95 DEG C, reaction 35min.
The mass percent that the phospholipids content of the oil behind step (1) ~ (4), unsaponifiable matter content and esterification carbon distribution account for oil quality is respectively 0.13%, 0.40% and 0.11%.
(5) dehydration reaction: first the grease through step (4) is squeezed into normal pressure dehydrating kettle, open fire in grease is removed, then the grease after normal pressure being dewatered, flash-evaporation dehydration still is drawn in by vacuum, hot steam is passed in flash-evaporation dehydration still heating jacket, heating jacket wall working temperature is 125 DEG C, and grease slides from flash-evaporation dehydration still top along heating jacket wall, and most of moisture content is sloughed.
(6) saponification is saltoutd reaction:
Oil after dehydration adds 20% sodium hydroxide solution under normal pressure 100 DEG C of constant temperature, sodium hydroxide and the waste oil mass ratio after dewatering are 1:2, ethylene glycol or the alcohol of 20ml is added in every gram of waste oil, to improve the boiling point of grease and to increase solubleness, controlling pH value is 9 ~ 10,1/3 of sodium hydroxide solution total amount is dropped into during beginning, after reaction 1h, dropwise add the half of remaining alkali lye, after reaction 1.5h, dropwise add residue alkali lye, add fashionable continuous stirring, in saponification process, moisture constantly evaporates, and needs suitable make up water.Can observe in reaction, during beginning, reaction mass forms emulsion, but carries out being converted into solid close to when completing in reaction.
After soap glue is formed, add while stirring while hot and turn the warm saturated aqueous common salt got ready in advance and carry out saltouing, leave standstill 2h, cooling, collects all white particles.The object of saltouing be salt adding after soap glue, the electric charge of soap glue and other impurity is neutralized, impels glue polymers to separate with water.
(7) lipid acid is refined: be dissolved in water by white particle, 90 ~ 100 DEG C of heated and stirred, and after dissolving completely, adjust ph is 8, and adds saturated acetic acid lead solution, produces and precipitates in a large number, leaves standstill cooled and filtered, retains precipitation.
(8) stearic acid and oleic acid extract: present industrial general employing methyl alcohol as extraction agent, although but the lower toxicity of methyl alcohol cost is larger.The present invention selects ethanol as extraction agent, and the concentration of ethanol is 80%, can reach the object be separated according to stearic acid with oleic acid different solubility in ethanol.Oleic acid solubleness is in ethanol much larger than stearic acid, and when adopting ethanol to extract stearic acid and oleic acid mixture, oleic acid is dissolved in liquid phase, and stearic acid is then separated out with crystal.Separated by filter operation, filter cake is then stearic acid, and liquid phase is through distillation process, and reclaim ethanol, residue is oleic acid.To add the industrial alcohol of 3g in every gram of oil, heating in water bath dissolves, and makes the transparent brown color of solution, then cool, then adularescent fish scale-like stearic acid crystallization, then carries out press filtration, and with appropriate cold washing with alcohol filter cake to pure white look, dry, obtain stearic acid.Namely filtrate obtain oleic acid product through Distillation recovery ethanol simultaneously.
The stearic saponification value of gained, acid number, moisture and mineral acid are respectively: 211mgKOH/g, 227mgKOH/g, 0.25% and 0.0012%.
The saponification value of gained oleic acid, acid number, moisture and mineral acid are respectively: 200mgKOH/g, 205 mgKOH/g, 0.20%, 0.0013%.
Comparative example:
By the pre-treatment of waste oil without step (1) ~ (4), directly carry out step (5) ~ (8), the oleic acid obtained and stearic acid.
The stearic saponification value of gained, acid number, moisture and mineral acid are respectively: 251mgKOH/g, 293mgKOH/g, 1.20% and 0.0030%.
The saponification value of gained oleic acid, acid number, moisture and mineral acid are respectively: 218mgKOH/g, 217mgKOH/g, 0.23%, 0.0038%.
To the above-mentioned explanation of the disclosed embodiments, professional and technical personnel in the field are realized or uses the present invention.To be apparent for those skilled in the art to the multiple amendment of these embodiments, General Principle as defined herein can without departing from the spirit or scope of the present invention, realize in other embodiments.Therefore, the present invention can not be restricted to these embodiments shown in this article, but will meet the widest scope consistent with principle disclosed herein and features of novelty.
Claims (4)
1. from waste cooking oil, extract a technique for oleic acid, it is characterized in that: comprise the following steps,
(1) removing impurity by means of precipitation: waste oil is left standstill 7 ~ 10 hours, perforated lower floor residue precipitation;
(2) hydration degum: add water by the oil processed through step (1), amount of water is 1.2 ~ 1.8% of oil quality, then under the constant temperature of 70 ~ 80 DEG C, reaction 35 ~ 45min;
(3) centrifugation: the oil through step (2) is carried out centrifugation, rotating speed is 3500 ~ 4500r/min, centrifugal 10 ~ 25min;
(4) decoloring reaction: add atlapulgite and water glass by the oil of step (3), while stir general heating, Heating temperature is 75 ~ 95 DEG C, reaction 35 ~ 55min, the mass ratio of described atlapulgite and water glass is 3.5 ~ 4.5:1, always adds quality for 8.5% ~ 9.5% of the oil quality after step (3) process;
(5) dehydration reaction: first the oil through step (4) is squeezed into normal pressure dehydrating kettle, Heating temperature is 125 DEG C;
(6) saponification is saltoutd reaction: the oil after step (5) dehydration adds 20% sodium hydroxide solution under normal pressure 100 DEG C of constant temperature stir, mass ratio 1:1.8 ~ 2.8 of sodium hydroxide solution and the oil after step (5) is dewatered, ethylene glycol or the alcohol of 20ml is added, until solution transforms is solid in every gram of waste oil; Add warm saturated aqueous common salt while hot while stirring to carry out saltouing, leaving standstill 2h, cooling, collects all white particles;
(7) lipid acid is refined: be dissolved in water by the white particle that step (6) is formed, 90 ~ 100 DEG C of heated and stirred, and after dissolving completely, adjust ph is 8, and adds saturated acetic acid lead solution, produces and precipitates in a large number, leaves standstill cooled and filtered, retains precipitation;
(8) oleic acid and stearic acid extract: add the ethanol that concentration is 80% in the precipitation formed in step (7) a metallic, add-on is the ethanol adding 3g in every gram of oil, and heating in water bath dissolves, make the transparent brown color of solution, then cool, stearic acid is then separated out with crystal, and residue is oleic acid.
2. a kind of technique extracting oleic acid from waste cooking oil according to claim 1, it is characterized in that: the amount of water in described step (2) is 1.5% of oil quality, temperature of reaction is 75 DEG C, and the reaction times is 40min.
3. a kind of technique extracting oleic acid from waste cooking oil according to claim 1, it is characterized in that: the atlapulgite in described step (4) and water glass mass ratio are 4:1, total mass is 9%, and temperature of reaction is 85 DEG C, and the reaction times is 45min.
4. a kind of technique extracting oleic acid from waste cooking oil according to claim 1, it is characterized in that: the feed postition of the sodium hydroxide solution in described step (6) is: dropwise add 1/3 of sodium hydroxide solution total amount during beginning, after reaction 1h, dropwise add the half of remaining alkali lye, after reaction 1.5h, dropwise add residue alkali lye.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510302013.9A CN104877761A (en) | 2015-06-04 | 2015-06-04 | Process for extracting oleic acid from waste cooking oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510302013.9A CN104877761A (en) | 2015-06-04 | 2015-06-04 | Process for extracting oleic acid from waste cooking oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104877761A true CN104877761A (en) | 2015-09-02 |
Family
ID=53945442
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510302013.9A Pending CN104877761A (en) | 2015-06-04 | 2015-06-04 | Process for extracting oleic acid from waste cooking oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104877761A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106318441A (en) * | 2016-10-13 | 2017-01-11 | 宁夏宝塔石化科技实业发展有限公司 | Diesel oil de-coloring agent as well as preparation method and de-coloring process thereof |
| CN107185720A (en) * | 2017-06-21 | 2017-09-22 | 湖北宜化江家墩矿业有限公司 | A kind of modified swill-cooked dirty oil production collophane collecting agent and method |
| CN109179688A (en) * | 2018-09-17 | 2019-01-11 | 南京大学 | A kind of denitrifying carbon source and preparation method thereof |
| CN111534381A (en) * | 2020-05-14 | 2020-08-14 | 广东锦坤实业有限公司 | Process equipment for producing oleic acid by using plant waste oil |
| CN113211681A (en) * | 2021-05-28 | 2021-08-06 | 广东伟艺抛磨材料有限公司 | Method for treating phase change waste in nylon wheel production |
-
2015
- 2015-06-04 CN CN201510302013.9A patent/CN104877761A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106318441A (en) * | 2016-10-13 | 2017-01-11 | 宁夏宝塔石化科技实业发展有限公司 | Diesel oil de-coloring agent as well as preparation method and de-coloring process thereof |
| CN107185720A (en) * | 2017-06-21 | 2017-09-22 | 湖北宜化江家墩矿业有限公司 | A kind of modified swill-cooked dirty oil production collophane collecting agent and method |
| CN109179688A (en) * | 2018-09-17 | 2019-01-11 | 南京大学 | A kind of denitrifying carbon source and preparation method thereof |
| CN111534381A (en) * | 2020-05-14 | 2020-08-14 | 广东锦坤实业有限公司 | Process equipment for producing oleic acid by using plant waste oil |
| CN113211681A (en) * | 2021-05-28 | 2021-08-06 | 广东伟艺抛磨材料有限公司 | Method for treating phase change waste in nylon wheel production |
| CN113211681B (en) * | 2021-05-28 | 2022-09-30 | 广东伟艺抛磨材料有限公司 | Method for treating phase change waste in nylon wheel production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104877761A (en) | Process for extracting oleic acid from waste cooking oil | |
| CN102492546B (en) | Rice bran oil refinement and byproduct production method | |
| CN103289816A (en) | Tea oil processing method and device special for tea oil processing method | |
| CN101473873A (en) | Industrial refining production method of rice bran oil and equipment thereof | |
| CN110294784B (en) | Method for extracting oryzanol by taking rice bran oil refined soapstock as raw material | |
| CN102766524B (en) | Method for squeezing edible tea seed oil at normal temperature | |
| CN102504947B (en) | Method for refining cottonseed mixed oil | |
| CN106929160B (en) | Method for refining vegetable oil wax | |
| CN102839049A (en) | Technical method of deacidifying vegetable fat | |
| CN104928023A (en) | Corn oil soap-free refining process | |
| CN101319168A (en) | Method for preparing wax tree wax with wax tree seed | |
| CN106833888A (en) | A kind of efficient method for acid stripping and refining of tea seed crude oil | |
| CN104611132A (en) | Acid reducing process of rice oil | |
| CN104830525B (en) | A kind of multi-stage countercurrent of antarctic krill oil continuously leaches and process for purification | |
| CN103865637B (en) | After carrying polyphenol, Semen Vitis viniferae produces the method for raisin seed oil | |
| CN103382413A (en) | Refining process for reducing content of MCPD in tea seed oil | |
| CN103773610A (en) | Method for preparing stearic acid and oleic acid from waste oil in kitchen garbage | |
| CN104232300A (en) | Method for refining mixed oil of microalgae DHA oil | |
| CN101519626A (en) | Process for extracting Alpha-linolenic acid from silkworm pupa crude oil | |
| CN101617720A (en) | Preparation method of plant oil from blackberry seeds | |
| CN104711112A (en) | Method for realization of combined production of high quality rice bran oil and ferulic acid from rice bran | |
| CN1299862A (en) | Cotton oil extracting and detoxicating process | |
| CN102766525B (en) | Method for squeezing tea seed oil at normal temperature | |
| CN101653173A (en) | Bunge pricklyash seed edible oil and production method thereof | |
| CN102766527B (en) | Method for squeezing and refining tea seed oil at low temperature |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20150902 |