CN1304545C - Method for preparing fatty acid through continuous hydrolyzing grease without catalysis in near critical aqueous medium - Google Patents
Method for preparing fatty acid through continuous hydrolyzing grease without catalysis in near critical aqueous medium Download PDFInfo
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- CN1304545C CN1304545C CNB2005100503340A CN200510050334A CN1304545C CN 1304545 C CN1304545 C CN 1304545C CN B2005100503340 A CNB2005100503340 A CN B2005100503340A CN 200510050334 A CN200510050334 A CN 200510050334A CN 1304545 C CN1304545 C CN 1304545C
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Abstract
The present invention discloses a method for preparing fatty acid through continuously hydrolyzing grease without catalysis in a water medium the near-critical state, which comprises the following steps: 1, according to the volume ratio of 0.25 to 1.2 between water and grease, water preheated by a preheater is mixed with grease, and the mixture enters a tubular reactor and is hydrolyzed for 5 to 60 minutes under the near-critical water condition of 250 to 350DEG C and 5 to 20MPa; 2, hydrolyzed products are cooled by a cooler and then are decompressed by a backpressure valve; 3, decompressed products are separated by a liquid-liquid separator, water phrases are used for recovering glycerol, and grease phrases are used for preparing fatty acid after being decompressed and distilled. The present invention has the advantages of continuous operation, short staying time of the grease in the tubular reactor, small volume of the reactor, high hydrolysis rate, little pollution, high quality of products and high concentration of glycerol in sweet water. In addition, besides palm oil as raw materials, the present invention can be used for processing acidic oil in oil sediment, waste grease in food industry, waste oil, etc.
Description
Technical field
The present invention relates to fatty acid, relate in particular to that grease does not have the method that the catalysis continuous hydrolysis prepares lipid acid in a kind of near critical aqueous medium.
Background technology
Lipid acid is important chemical material, it is one of basic material of tensio-active agent, with it is that starting raw material can prepare multiple negatively charged ion, nonionic, positively charged ion and amphoterics, be widely used in industry such as light textile, washing, rubber, makeup, plastics, papermaking, medicine, food, oil, synthon, process hides, ore dressing, machinery, demand is growing.In addition, be important basic grease chemical article by the set out Fatty Alcohol(C12-C14 and C12-C18), fatty acid methyl ester, aliphatic amide etc. of preparation of lipid acid, its demand is also in continuous growth.
The source of lipid acid mainly contains three approach: the one, and the animal-plant oil hydrolysis, the 2nd, extract in the papermaking wastewater Yatall MA, the 3rd, from the petrochemical materials synthetic fatty acid.
Total standing stock of petroleum resources have certain restriction, are not nexhaustible, and a large amount of uses of Mineral resources such as oil and coal have brought serious pollution problem.From resource, oil is just superior not as reproducible natural fats and oils.With the product that natural fats and oils is made, its biological degradability, the pollution to environment, pungency, security than being that the product made of raw material is good with the oil, are raw material production lipid acid so worldwide be devoted to development with the natural fats and oils all.
At present, the animal-plant oil hydrolysis has become the main source that lipid acid is produced.The fat hydrolysis method can be divided into gap method and continuous processing by operating method; By whether having catalyzer can be divided into no catalysis and catalysis (adopting acid, alkali, enzyme etc.) being arranged; By working pressure can be divided into low pressure (170～190 ℃, 0.8～1.2MPa), middle pressure (230 ℃, 2.5MPa) and high pressure (250～260 ℃, 5.5～6.0MPa) hydrolysis method.At present domestic still based on low pressure interstitial water solution, there are problems such as energy consumption is big, hydrolysis time is long, technological process is unstable, quality product is relatively poor in this method.
(Near Critical Water NCW) typically refers to the compressed liquid water of temperature between 250～350 ℃ to near-critical water.Water has following three key properties in this zone:
1) depress at saturated vapo(u)r, the ionization constant of NCW has a maximum value to be about 10 near 275 ℃
-11(mol/kg)
2, its value is 1000 times of normal temperature and pressure water, and ionization constant increases the [H among the NCW with the increase of pressure
3O
+] and [OH
-] concentration is near weak acid or weak base, self has the function of acid catalysis and base catalysis, therefore can make some acid-base catalyzed reaction needn't add acid base catalysator, thereby avoid the neutralization of soda acid, the operations such as processing of salt;
2) depress at saturated vapo(u)r, the specific inductivity of 20 ℃ of water is 80.1, and has only 23.5 275 ℃ the time.Although the specific inductivity of NCW is still bigger, solubilized even ionized salts, enough little of dissolved organic matter, (275 ℃ of saturated vapo(u)rs density of depressing water is 0.76g/cm to add that the density of NCW is big
3, the specific inductivity of NCW, density and acetone are close), so NCW has extraordinary solubility property, has the characteristic of dissolved organic matter and inorganics simultaneously.This can carry out the building-up reactions in many NCW media in homogeneous phase, thereby eliminates resistance to mass transfer, improves speed of response, and the reaction back only needs simple cooling just can realize oily water separation simultaneously, and water can be recycled;
3) physicochemical property such as the specific inductivity of NCW, ion-product constant, density, viscosity, spread coefficient, solubleness are adjustable continuously in the scope of broad with temperature, pressure, the rerum natura that is NCW has controllability (tuning property), therefore as reaction medium, NCW has different solvent properties and reactivity worth at different states.
The applied research of reacting among the NCW comprises that offal treatment, macromolecular material recycle, inorganic materials are synthetic, gelatin liquefaction and biomass as resources etc., to going deep into that these three characteristics are familiar with, make the Application Areas among the NCW constantly obtain enlarging just because of people.The present invention is applied in the characteristic of NCW in the greasy hydrolysis, thereby realizes greasy no catalysis, continuous, hydrolysis fast.
Summary of the invention
The purpose of this invention is to provide a kind of green, grease does not have the method that the catalysis continuous hydrolysis prepares lipid acid in the near critical aqueous medium efficiently.
Grease does not have the catalysis continuous hydrolysis to prepare the step of method of lipid acid as follows in the near critical aqueous medium:
1) water mixes than 0.25～1.2 by the water oil volume with grease after the preheater preheating, enters tubular reactor, hydrolysis 5～60min under 250～350 ℃, the near clinical water condition of 5～20MPa;
2) hydrolyzed product reduces pressure through back pressure valve after the water cooler cooling again;
3) post-decompression product separates through the liquid liquid/gas separator, and water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.
Wherein the water oil volume is good than 0.4～0.8.
Advantage of the present invention:
1) operate continuously;
2) residence time of grease in tubular reactor short, dropped to less than 1 hour by 8 hours of gap method, can reduce the generation of side reaction;
3) reactor volume is little;
4) fat hydrolysis rate height;
5) owing to adopt no catalysis technique, therefore pollute few;
6) color and luster of quality product height, particularly product is good;
7) glycerol concentration height in the sugar water (referring to the glycerinated aqueous solution that fat hydrolysis obtains);
8) raw material can be handled oil foot acidifying oil (oil foot that produces in the crude oil alkali refining process obtains through acidifying), the waste grease of catering industry, trench wet goods except that plam oil, animal-plant oil, plant oil leftover, therefore can also produce good social benefit.
Description of drawings
Accompanying drawing is that grease does not have the process flow diagram that the catalysis continuous hydrolysis prepares the lipid acid method in the near critical aqueous medium.
Embodiment
Embodiment 1
By water oil volume ratio is 1, water mixes with plam oil after preheater is preheated to 270 ℃, enter tubular reactor, hydrolysis 60min (hydrolysis time is by flow and the control of reactor size) under 250 ℃, the near clinical water condition of 5MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99%.
Embodiment 2
By water oil volume ratio is 0.75, water mixes with oil foot acidifying oil after preheater is preheated to 270 ℃, enter tubular reactor, hydrolysis 40min under 250 ℃, the near clinical water condition of 5MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99.5%.
Embodiment 3
By water oil volume ratio is 0.5, water mixes with sewer oil after preheater is preheated to 280 ℃, enter tubular reactor, hydrolysis 40min under 260 ℃, the near clinical water condition of 6MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 97%.
Embodiment 4
By water oil volume ratio is 0.5, water mixes with plam oil after preheater is preheated to 280 ℃, enter tubular reactor, hydrolysis 30min under 260 ℃, the near clinical water condition of 6MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 98%.
Embodiment 5
By water oil volume ratio is 0.6, water is preheated to after 300 ℃ through preheater and mixes with the waste grease of catering industry, enter tubular reactor, hydrolysis 20min under 280 ℃, the near clinical water condition of 8MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 97.5%.
Embodiment 6
By water oil volume ratio is 0.4, water mixes with oil foot acidifying oil after preheater is preheated to 300 ℃, enter tubular reactor, hydrolysis 10min under 280 ℃, the near clinical water condition of 8MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99%.
Embodiment 7
By water oil volume ratio is 0.25, water mixes with oil foot acidifying oil after preheater is preheated to 320 ℃, enter tubular reactor, hydrolysis 10min under 300 ℃, the near clinical water condition of 10MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 97%.
Embodiment 8
By water oil volume ratio is 0.5, water mixes with plam oil after preheater is preheated to 310 ℃, enter tubular reactor, hydrolysis 15min under 300 ℃, the near clinical water condition of 10MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99.5%.
Embodiment 9
By water oil volume ratio is 0.6, water is preheated to after 330 ℃ through preheater and mixes with the waste grease of catering industry, enter tubular reactor, hydrolysis 10min under 320 ℃, the near clinical water condition of 16MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 98.5%.
Embodiment 10
By water oil volume ratio is 0.5, water mixes with sewer oil after preheater is preheated to 330 ℃, enter tubular reactor, hydrolysis 12min under 320 ℃, the near clinical water condition of 16MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99%.
Embodiment 11
By water oil volume ratio is 1.2, water mixes with plam oil after preheater is preheated to 350 ℃, enter tubular reactor, hydrolysis 5min under 350 ℃, the near clinical water condition of 20MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99.5%.
Embodiment 12
By water oil volume ratio is 1, water mixes with sewer oil after preheater is preheated to 350 ℃, enter tubular reactor, hydrolysis 5min under 350 ℃, the near clinical water condition of 20MPa, hydrolyzed product is after the water cooler cooling, again through the back pressure valve decompression, after the separation of liquid liquid/gas separator, water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.Getting the raw material percent hydrolysis is 99%.
Claims (4)
1. grease does not have the method that the catalysis continuous hydrolysis prepares lipid acid in the near critical aqueous medium, it is characterized in that step is as follows:
1) water mixes than 0.25～1.2 by the water oil volume with grease after the preheater preheating, enters tubular reactor, hydrolysis 5～60min under 250～350 ℃, the near clinical water condition of 5～20MPa;
2) hydrolyzed product reduces pressure through back pressure valve after the water cooler cooling again;
3) post-decompression product separates through the liquid liquid/gas separator, and water is used for glycerine and reclaims, and oil phase gets lipid acid after underpressure distillation.
2. grease does not have the method that the catalysis continuous hydrolysis prepares lipid acid in a kind of near critical aqueous medium according to claim 1, it is characterized in that described hydrolysis temperature is 250～300 ℃.
3. grease does not have the method that the catalysis continuous hydrolysis prepares lipid acid in a kind of near critical aqueous medium according to claim 1, it is characterized in that described grease is the waste grease of plam oil, oil foot acidifying oil, sewer oil or catering industry.
4. grease does not have the method that the catalysis continuous hydrolysis prepares lipid acid in a kind of near critical aqueous medium according to claim 1, it is characterized in that described water oil volume ratio is 0.4～0.8.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100503340A CN1304545C (en) | 2005-05-16 | 2005-05-16 | Method for preparing fatty acid through continuous hydrolyzing grease without catalysis in near critical aqueous medium |
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|---|---|---|---|
| CNB2005100503340A CN1304545C (en) | 2005-05-16 | 2005-05-16 | Method for preparing fatty acid through continuous hydrolyzing grease without catalysis in near critical aqueous medium |
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| CN1304545C true CN1304545C (en) | 2007-03-14 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN100372918C (en) * | 2006-02-10 | 2008-03-05 | 杨解定 | Mixed fatty acid and its prepn process and application |
| CN100398633C (en) * | 2006-05-19 | 2008-07-02 | 浙江大学 | Method for non-catalytic lanolin hydrolyzed preparation of lanolin acid and lanolin alcohol using in near critical water medium |
| CN101928644B (en) * | 2010-09-07 | 2012-08-29 | 昆明理工大学 | Method for preparing fatty acid by illegal cooking oil |
| CN102827699A (en) * | 2012-09-14 | 2012-12-19 | 哈尔滨工业大学 | Method for hydrolyzing soap stock to extract fatty acid by adopting sub-critical acetic acid way |
| CN105107232B (en) * | 2015-09-17 | 2017-03-29 | 湖州新奥特医药化工有限公司 | A kind of pre- cold mould refrigerated separation structure |
| CN112778119A (en) * | 2021-01-13 | 2021-05-11 | 杭州洁汉化工有限公司 | Green aqueous phase solvent-free high-purity synthesis method of palmitoylethanolamide |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1544595A (en) * | 2003-11-27 | 2004-11-10 | 陈天晓 | Method for low-pressure continuous hydrolysis preparation of fatty acid |
| WO2005005584A1 (en) * | 2003-07-10 | 2005-01-20 | Akzo Nobel N.V. | Process for preparing purified fatty acids |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005005584A1 (en) * | 2003-07-10 | 2005-01-20 | Akzo Nobel N.V. | Process for preparing purified fatty acids |
| CN1544595A (en) * | 2003-11-27 | 2004-11-10 | 陈天晓 | Method for low-pressure continuous hydrolysis preparation of fatty acid |
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