CN101880603A - Method for preparing low condensation point biodiesel from high acid value oil - Google Patents
Method for preparing low condensation point biodiesel from high acid value oil Download PDFInfo
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Abstract
The invention discloses a method for preparing low condensation point biodiesel from high acid value oil. Animal and vegetable oils with the acid value higher than 80mgKOH/g serving as a raw material and mixed alcohol of methanol, ethanol and isopropanol undergo esterification and interesterification two-step reaction to prepare the low condensation point biodiesel. The intersolubiltiy of the oil and the methanol is improved by the ethanol so as to promote the methyl esterification reaction; meanwhile, the product contains a small amount of fatty acid ethyl esters, and new solid catalysts of tungsten molybdophosphate and phosphotungstic acidesterification replace concentrated sulfuric acid in the esterification reaction; and in the interesterification reaction, the ethanol and the isopropanol promote the conversion of glyceride, and simultaneously the product contains partial fatty acid ethyl esters and branched-chain aliphatic esters. Therefore, the reaction is easy to carry out, the cold flow properties of the biodiesel can be improved and the condensation point of the biodiesel can be reduced.
Description
Technical field
The invention belongs to the preparation method of biofuel, more particularly, the present invention relates to a kind of method for preparing low freezing point biodiesel by high acid value oil.
Background technology
Because pressing for of the order of fossil fuel resource benefit exhaustion and environmental protection, the exploitation of clean energy more and more is subject to people's attention.The energy research personnel of countries in the world try to explore to develop alternative fuel and renewable energy source from the angle of environment protection and resource strategy, and biofuel is exactly wherein a kind of.
In the prior art, produce biofuel and generally carry out alcoholysis reaction by grease and methyl alcohol and obtain, this mainly is because the big speed of response of methyl alcohol polarity is very fast, and low price.With the biofuel of grease and methyl alcohol preparation, its most of performance is near petrifaction diesel, but its low-temperature fluidity and petrifaction diesel have certain gap, and its low temperature flowability of biofuel of the sewer oil preparation of usefulness high acid value is just poorer especially.The method of improving the biodiesel lower-temperature fluidity energy mainly comprises adds pour point depressant and filter out two kinds of a part of saturated fatty acid methyl esters under freezing, and the former adopts the pour point depressant of petrifaction diesel to realize; The latter can reduce condensation point, but loses nearly 20% fatty acid methyl ester.
Patent CN101126031 is that the vegetable and animals oils of 55～160 high acid values and the vitriol oil of catalytic amount mix with methyl alcohol and branched-chain alcoho with acid number, at 50～95 ℃, reacted 1.5～10 hours, obtain to reduce the biofuel of condensation point, this method high acid value vegetable and animals oils is reacted under an acidic catalyst condition, glyceryl ester wherein is to be difficult to be converted into fully methyl esters or branched fatty acid ester, and the unsaturated fatty acids in the grease is very easily influenced the quality of biofuel by vitriol oil oxidation simultaneously.Patent CN18767664A adopts two-step approach to prepare biofuel with animal oil, and the first step is made catalyzer with the vitriol oil at normal temperatures and pressures, makes most of glyceryl ester and part free fatty acids and isopropanol reaction generate isopropyl fatty acid ester; Second step is at comparatively high temps and add and depress, and adopts concentrated sulfuric acid catalyst equally and adds the yield that excessive Virahol improves isopropyl ester, but cause cost too high with excessive Virahol.The vegetables oil of human methyl alcohol such as Liao Li and ethanol and low acid number carries out transesterify single step reaction legal system and gets biofuel under the effect of basic catalyst.Other patent all is that the method for using for reference petrifaction diesel pour point depression point is carried out, and promptly adds pour point depressant condensation point and its low-temperature fluidity of raising to reduce biofuel in biofuel.
How to utilize the biofuel of the low condensation point of high acid value oil preparation, do not see relevant report so far as yet.This is one is worth the further investigation technical barrier.
Summary of the invention
The objective of the invention is at the deficiencies in the prior art, it is the method for feedstock production low freezing point biodiesel that a kind of vegetable and animals oils with high acid value is provided.
Purpose of the present invention is achieved by following technical proposals.
* except as otherwise noted, the percentage ratio that is adopted among the present invention is mass percent.
The invention provides a kind of is the method for feedstock production low freezing point biodiesel with high acid value oil, and this method may further comprise the steps:
1. acid number is carried out pre-treatment greater than the vegetable and animals oils of 80mgKOH/g
The high acid value vegetable and animals oils is mixed stirring 10～30 minutes with concentration 5%～10% alum liquor 1: 0.5 by volume～1, temperature keeps 60～80 ℃, left standstill 1～3 hour, isolate water after the layering, with oil phase under 110 ℃～115 ℃, dewatering to the massfraction of water is lower than 0.5%, pre-treatment oil.
2. the esterification of pre-treatment oil
The massfraction of alcohol oil is than 1～3: 1, and alcohol is methyl alcohol and alcoholic acid alcohol mixture; Catalyst levels 0.5%～1.5%, catalyzer are selected from a kind of in P-Mo-Wo acid, phospho-wolframic acid, Tungsten oxide 99.999 or the zirconium white or their mixture; Under 60～85 ℃ temperature, stirring reaction 30～60 minutes gets esterification products.Decompression is reclaimed alcohol down, and standing demix is discharged water-glycerine mutually, steams moisture and reclaims solid acid; Oil phase water consumption and oil mass volume ratio 0.5～1: 1 washed twice, the temperature of washing system is 70～90 ℃, washing time 20～30 minutes; The esterification products of washing oil and dehydration under 110～115 ℃ are as the raw material of transesterification reaction.
3. esterification products is carried out transesterification reaction
The massfraction of alcohol oil is than 3～8: 1, and catalyzer is selected from KOH, K
2O-Al
2O
3Or MgO-Al
2O
3In a kind of, or their mixture, catalyst levels 0.5～1.5%; Under 65～75 ℃ temperature, stirring reaction 60～90 minutes gets coarse biodiesel.Alcohol required in the reaction preferentially is selected from methyl alcohol, ethanol or Virahol.
4. coarse biodiesel is refining
Coarse biodiesel after esterification and the transesterification reaction is under reduced pressure reclaimed alcohol, oily standing demix, the upper strata is the product biofuel, lower floor is that glycerine and catalyst layer are discharged; Bio-diesel layer is re-refined, and promptly obtains required low freezing point biodiesel.
Reaction mechanism of the present invention
The present invention is a raw material with the vegetable and animals oils that acid number is higher than 80mgKOH/g, with methyl alcohol and ethanol, Virahol alcohol mixture, prepares low freezing point biodiesel by esterification, transesterify two-step reaction method.The mutual solubility that increases grease and methyl alcohol by ethanol promotes esterification reaction of organic acid, makes simultaneously and contains part little fat acetoacetic ester in the product, and esterification adopts P-Mo-Wo acid and phospho-wolframic acid novel solid catalyzer to substitute the vitriol oil; Transesterification reaction promotes the conversion of glyceryl ester to make and contain partial fatty acid ethyl ester and branched fatty acid ester in the product simultaneously with ethanol and Virahol.Thereby make reaction be easy to carry out, can improve the low temperature flowability of biofuel again and reduce its condensation point.
Compared with prior art, the present invention has following outstanding advantage:
1. the oil that is higher than 80mgKOH/g with acid number is raw material and methyl alcohol, ethanol synthesis, produces the biofuel of low condensation point, and the condensation point of product can reduce by 3～8 ℃, and the low-temperature fluidity of product improves, and the product calorific value can improve 500～1000cal/g.
2. adopt esterification, transesterify two-step reaction to produce low freezing point biodiesel.Esterification is that free fatty acids and alcohol reaction are generated fatty acid ester, and the acid number of system is reduced to below 2.0; Transesterification reaction is that glycerin fatty acid ester is converted into fatty acid methyl ester, fatty-acid ethyl ester, isopropyl fatty acid ester, and the acid number of product reaches below 0.6.
3. by adding ethanol, Virahol, improved the mutual solubility of high acid value oil, promoted esterification reaction of organic acid, reduced the condensation point of biofuel, improved the low-temperature fluidity of biofuel with methyl alcohol.
4. esterification is made catalyzer with solid acid P-Mo-Wo acid, phospho-wolframic acid, Tungsten oxide 99.999, zirconium white, the transformation efficiency height of reaction, and speed of response is very fast, has improved the stability of esterification products simultaneously, and the recyclable utilization of catalyzer.
5. adopt after esterification and the transesterification reaction with each washed twice of hot water, can improve the transparency of biofuel and improve its low-temperature fluidity.
Embodiment
In order to make purpose of the present invention, technical scheme and advantage clearer, by the following examples the present invention is further elaborated.Should be appreciated that specific embodiment described herein only in order to explanation the present invention, and be not used in qualification the present invention.
Embodiment 1
1. the pre-treatment of sewer oil: getting the 200g acid number is 121.5mgKOH/g, water ratio is that 3% sewer oil and 100ml concentration are 8% alum liquor, join the beaker of 800ml, be heated to 65～70 ℃, stir 20min, pour the separating funnel standing demix into and isolate lower floor and contain colloid and impurity, the upper strata grease is put in the round-bottomed flask of 1000ml and is dewatered under 110～115 ℃ to water content 0.4%, the 191.4g grease.
2. greasy esterification: pretreated grease and 150ml methyl alcohol, 50ml ethanol and 1.2g P-Mo-Wo acid are joined the 1000ml there-necked flask, heat 65～72 ℃, stirring reaction 60min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's catalyzer water, pour crucible into and put oven for drying moisture and get the 0.98g solid acid.Oil reservoir is with 150g distilled water wash twice, and oil is put in the round-bottomed flask of 1000ml and dewatered under 110～115 ℃ to water content 0.3%, the 192.5g esterification products.Reaction product acid number 1.8mgKOH/g.
3. the transesterification reaction of esterification products: esterification products and 600ml methyl alcohol, 150ml ethanol, 100ml Virahol and 1.0g potassium hydroxide are joined the 2000ml there-necked flask, heat 70～75 ℃, stirring reaction 1h, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's glycerine.Oil reservoir is with 150g distilled water wash twice, and oil is put in the round-bottomed flask of 1000ml and dewatered under 110～115 ℃ to water content 0.3%, the 191.2g biofuel.Product acid number 0.6mgKOH/g, condensation point-4 ℃.
Embodiment 2
1. the pre-treatment of palm waste oil: getting the 100g acid number is 119.8mgKOH/g, water ratio is that 3% palm waste oil and 60ml concentration are 6% alum liquor, join the beaker of 500ml, be heated to 65～70 ℃, stir 20min, pour the separating funnel standing demix into and isolate lower floor and contain colloid and impurity, the upper strata grease is put in the round-bottomed flask of 500ml and is dewatered under 110～115 ℃ to water content 0.4%, the 92.6g grease.
2. greasy esterification: pretreated grease and 60ml methyl alcohol, 20ml ethanol and 1.0g P-Mo-Wo acid are joined the 500ml there-necked flask, heat 65～70 ℃, stirring reaction 40min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's catalyzer water, pour crucible into and put oven for drying moisture and get the 0.88g solid acid.Oil reservoir is with 60g distilled water wash twice, and oil is put in the round-bottomed flask of 500ml and dewatered under 110～115 ℃ to water content 0.3%, the 91.8g esterification products.Reaction product acid number 1.7mgKOH/g.
3. the transesterification reaction of esterification products: esterification products and 400ml methyl alcohol, 50ml ethanol, 60ml Virahol and 0.7g potassium hydroxide are joined the 2000ml there-necked flask, heat 68～75 ℃, stirring reaction 70min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's glycerine.Oil reservoir is with 80g distilled water wash twice, and oil is put in the round-bottomed flask of 500ml and dewatered under 110～115 ℃ to water content 0.2%, the 90.5g biofuel.Product acid number 0.5mgKOH/g, condensation point-7 ℃.
Embodiment 3
1. the pre-treatment of sewer oil: getting the 100g acid number is 181.4mgKOH/g, water ratio is that 2% sewer oil and 70ml concentration are 5% alum liquor, join the beaker of 500ml, be heated to 65～70 ℃, stir 20min, pour the separating funnel standing demix into and isolate lower floor and contain colloid and impurity, the upper strata grease is put in the round-bottomed flask of 500ml and is dewatered under 110～115 ℃ to water content 0.4%, the 92.8g grease.
2. greasy esterification: pretreated grease and 70ml methyl alcohol, 20ml ethanol and 1.0g phospho-wolframic acid are joined the 500ml there-necked flask, heat 65～70 ℃, stirring reaction 30min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's catalyzer water, pour crucible into and put oven for drying moisture and get the 0.89g solid acid.Oil reservoir is with 60g distilled water wash twice, and oil is put in the round-bottomed flask of 500ml and dewatered under 110～115 ℃ to water content 0.3%, the 92.0g esterification products.Reaction product acid number 1.8mgKOH/g.
3. the transesterification reaction of esterification products: esterification products and 450ml methyl alcohol, 40ml ethanol, 60ml Virahol and 0.6g potassium hydroxide are joined the 2000ml there-necked flask, heat 68～75 ℃, stirring reaction 80min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's glycerine.Oil reservoir is with 80g distilled water wash twice, and oil is put in the round-bottomed flask of 500ml and dewatered under 110～115 ℃ to water content 0.3%, the 91.3g biofuel.Product acid number 0.7mgKOH/g, condensation point-2 ℃.
Embodiment 4
1. the pre-treatment of swill oil: getting the 150g acid number is 140.2mgKOH/g, water ratio is that 1.5% swill oil and 120ml concentration are 10% alum liquor, join the beaker of 500ml, be heated to 65～70 ℃, stir 25min, pour the separating funnel standing demix into and isolate lower floor and contain colloid and impurity, the upper strata grease is put in the round-bottomed flask of 500ml and is dewatered under 110～115 ℃ to water content 0.3%, the 137.3g grease.
2. greasy esterification: pretreated grease and 160ml methyl alcohol, 40ml ethanol and 0.6g P-Mo-Wo acid and 0.5g phospho-wolframic acid are joined the 1000ml there-necked flask, heat 65～75 ℃, stirring reaction 50min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's catalyzer water, pour crucible into and put oven for drying moisture and get the 0.93g solid acid.Oil reservoir is with 80g distilled water wash twice, and oil is put in the round-bottomed flask of 500ml and dewatered under 110～115 ℃ to water content 0.3%, the 138.8g esterification products.Reaction product acid number 1.5mgKOH/g.
3. the transesterification reaction of esterification products: esterification products and 650ml methyl alcohol, 50ml ethanol, 80ml Virahol and 1.2g potassium hydroxide are joined the 2000ml there-necked flask, heat 68～75 ℃, stirring reaction 90min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's glycerine.Oil reservoir is with 100g distilled water wash twice, and oil is put in the round-bottomed flask of 500ml and dewatered under 110～115 ℃ to water content 0.2%, the 138.5g biofuel.Product acid number 0.4mgKOH/g, condensation point-6 ℃.
Embodiment 5
1. the pre-treatment of waste cooking oil: getting the 200g acid number is 89.7mgKOH/g, water ratio is that 2.2% waste cooking oil and 120ml concentration are 5% alum liquor, join the beaker of 800ml, be heated to 65～70 ℃, stir 20min, pour the separating funnel standing demix into and isolate lower floor and contain colloid and impurity, the upper strata grease is put in the round-bottomed flask of 1000ml and is dewatered under 110～115 ℃ to water content 0.4%, the 192.6g grease.
2. greasy esterification: pretreated grease and 160ml methyl alcohol, 60ml ethanol and 1.0g P-Mo-Wo acid and 0.4g phospho-wolframic acid are joined the 1000ml there-necked flask, heat 65～72 ℃, stirring reaction 60min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's catalyzer water, pour crucible into and put oven for drying moisture and get the 1.21g solid acid.Oil reservoir is with 140g distilled water wash twice, and oil is put in the round-bottomed flask of 1000ml and dewatered under 110～115 ℃ to water content 0.3%, the 193.4g esterification products.Reaction product acid number 1.3mgKOH/g.
3. the transesterification reaction of esterification products: esterification products and 600ml methyl alcohol, 80ml ethanol, 120ml Virahol and 1.2g potassium hydroxide are joined the 2000ml there-necked flask, heat 70～75 ℃, stirring reaction 80min, decompression steams unreacted alcohol, oil is put the separating funnel standing demix, give off lower floor's glycerine.Oil reservoir is with 150g distilled water wash twice, and oil is put in the round-bottomed flask of 1000ml and dewatered under 110～115 ℃ to water content 0.3%, the 193.2g biofuel.Product acid number 0.5mgKOH/g, condensation point-7 ℃.
The above only is preferred embodiment of the present invention, not in order to restriction the present invention, all any modifications of being done within the spirit and principles in the present invention, is equal to and replaces and improvement etc., all should be included within protection scope of the present invention.
Claims (2)
1. one kind is the method for feedstock production low freezing point biodiesel with high acid value oil, it is characterized in that, described method may further comprise the steps:
(1) high acid value oil is mixed stirring 10～30 minutes with concentration 5%～l0% alum liquor 1: 0.5 by volume～1, temperature keeps 60～80 ℃, left standstill 1～3 hour, isolate water after the layering, with oil phase under 110 ℃～115 ℃, dewatering to the massfraction of water is lower than 0.5%, pre-treatment oil;
(2) massfraction of alcohol oil is than 1～3: 1, and alcohol is methyl alcohol and alcoholic acid alcohol mixture; Catalyst levels 0.5%～l.5%, catalyzer are selected from a kind of in P-Mo-Wo acid, phospho-wolframic acid, Tungsten oxide 99.999 or the zirconium white or their mixture; Under 60～85 ℃ temperature, stirring reaction 30～60 minutes gets esterification products; Decompression is reclaimed alcohol down, and standing demix is discharged water-glycerine mutually, steams moisture and reclaims solid acid; Oil phase water consumption and oil mass volume ratio 0.5～1: 1 washed twice, the temperature of washing system is 70～90 ℃, washing time 20～30 minutes; The esterification products of washing oil and dehydration under 110～115 ℃ are as the raw material of transesterification reaction;
(3) massfraction of alcohol oil is than 3～8: 1, and catalyzer is selected from KOH, K
2O-Al
2O
3Or MgO-Al
2O
3In a kind of, or their mixture, catalyst levels 0.5～1.5%; Under 65～75 ℃ temperature, stirring reaction 60～90 minutes gets coarse biodiesel; Required alcohol is selected from methyl alcohol, ethanol or Virahol in the reaction;
(4) coarse biodiesel after esterification and the transesterification reaction is under reduced pressure reclaimed alcohol, oily standing demix, the upper strata is the product biofuel, lower floor is that glycerine and catalyst layer are discharged; Bio-diesel layer is re-refined, and promptly obtains required low freezing point biodiesel.
2. method according to claim 1 is characterized in that, described high acid value oil is the oil of acid number greater than 80mgKOH/g, and it is selected from a kind of in sewer oil, palm waste oil, swill oil or the waste cooking oil.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102226134A (en) * | 2011-05-12 | 2011-10-26 | 福建漳州鼎能生物科技有限公司 | Method for producing biodiesel by using waste oil |
| CN103923751A (en) * | 2014-04-24 | 2014-07-16 | 广东产品质量监督检验研究院 | Method for preparing biodiesel through illegal cooking oil and waste gas VOC (volatile organic compound) in coating production |
| CN104774695A (en) * | 2015-04-13 | 2015-07-15 | 江苏佳华新材料科技有限公司 | Preparation method of low-freezing diesel ester-type antiwear additive |
| CN105001998A (en) * | 2015-06-05 | 2015-10-28 | 常州大学 | Method for lowering condensation point of biodiesel |
| CN106244337A (en) * | 2016-08-03 | 2016-12-21 | 佛山市盈合电力燃料有限公司 | A kind of biodiesel for car use |
| CN113105935A (en) * | 2021-02-25 | 2021-07-13 | 安徽中天石化股份有限公司 | Carbonate type modified vegetable oil base oil and preparation method thereof |
| CN113493722A (en) * | 2021-06-29 | 2021-10-12 | 江西尊创新能源有限公司 | Method for removing colloid in acidified oil |
| CN113528236A (en) * | 2021-06-29 | 2021-10-22 | 江西尊创新能源有限公司 | Method for removing colloid in hogwash oil |
| CN115335355A (en) * | 2020-04-07 | 2022-11-11 | 巴斯夫欧洲公司 | Energy-saving production of biodiesel from natural or industrial waste oil |
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| CN1415705A (en) * | 2001-10-30 | 2003-05-07 | 中国石油化工股份有限公司 | Method for producing good quality diesel oil |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102226134A (en) * | 2011-05-12 | 2011-10-26 | 福建漳州鼎能生物科技有限公司 | Method for producing biodiesel by using waste oil |
| CN103923751A (en) * | 2014-04-24 | 2014-07-16 | 广东产品质量监督检验研究院 | Method for preparing biodiesel through illegal cooking oil and waste gas VOC (volatile organic compound) in coating production |
| CN103923751B (en) * | 2014-04-24 | 2015-05-20 | 广东产品质量监督检验研究院 | Method for preparing biodiesel through illegal cooking oil and waste gas VOC (volatile organic compound) in coating production |
| CN104774695A (en) * | 2015-04-13 | 2015-07-15 | 江苏佳华新材料科技有限公司 | Preparation method of low-freezing diesel ester-type antiwear additive |
| CN105001998A (en) * | 2015-06-05 | 2015-10-28 | 常州大学 | Method for lowering condensation point of biodiesel |
| CN106244337A (en) * | 2016-08-03 | 2016-12-21 | 佛山市盈合电力燃料有限公司 | A kind of biodiesel for car use |
| CN115335355A (en) * | 2020-04-07 | 2022-11-11 | 巴斯夫欧洲公司 | Energy-saving production of biodiesel from natural or industrial waste oil |
| CN113105935A (en) * | 2021-02-25 | 2021-07-13 | 安徽中天石化股份有限公司 | Carbonate type modified vegetable oil base oil and preparation method thereof |
| CN113493722A (en) * | 2021-06-29 | 2021-10-12 | 江西尊创新能源有限公司 | Method for removing colloid in acidified oil |
| CN113528236A (en) * | 2021-06-29 | 2021-10-22 | 江西尊创新能源有限公司 | Method for removing colloid in hogwash oil |
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Application publication date: 20101110 |