CN102382716A - Method and equipment for preparing biodiesel with high-acid-value waste oil - Google Patents
Method and equipment for preparing biodiesel with high-acid-value waste oil Download PDFInfo
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- CN102382716A CN102382716A CN2010102712962A CN201010271296A CN102382716A CN 102382716 A CN102382716 A CN 102382716A CN 2010102712962 A CN2010102712962 A CN 2010102712962A CN 201010271296 A CN201010271296 A CN 201010271296A CN 102382716 A CN102382716 A CN 102382716A
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The invention discloses a method and equipment for preparing biodiesel with high-acid-value waste oil, wherein the method includes steps for high-acid-value waste animal oil: a hydrolysis for generating fatty acid, b separation for aqueous fatty acid, c dehydration for the aqueous fatty acid, d esterification with methyl alcohol, and e flashing for separating the methyl alcohol and obtaining the biodiesel (fatty acid methyl ester). The method and the equipment have the advantages that catalysts and washing are omitted in the whole reaction process, the number of pieces of the equipment is decreased obviously, reaction and separation steps are fewer, less waste water and waste gas are emitted, and product quality is stable.
Description
Technical field
The present invention relates to the technical field that biofuel is made, specifically a kind ofly produce method of bio-diesel oil and equipment with the peracid value waste oil.
Background technology
Real raw material in China's production biofuel is the peracid value waste oil, and its acid value is generally about 100, and its main composition is following; Fatty acid glycerine ester content 48%, fatty acid content 47%, non-lipid impurity 5%; Conventional production process is the two-step acid-alkali method; Raw material will carry out pre-treatment earlier and remove non-lipid impurity, and the first step is made catalyzer with acid, and lipid acid in the raw material and methyl alcohol carry out esterification; Washing separates an acidic catalyst, drying and dehydrating then.Second step was made catalyzer with alkali, and raw material that the first step reacting drying is good and methyl alcohol carry out transesterification reaction, and washing separates basic catalyst again, and drying and dehydrating obtains refined biometric diesel oil (fatty acid methyl ester) after the rectifying.Find out that thus common process Reaction Separation step is many, wastewater flow rate is big, and the side reaction of doing the catalyzer generation with soda acid is many, and product yield is low, unstable product quality.
Summary of the invention
In order to solve the problems referred to above that exist in the prior art, it is high to the invention provides a kind of yield rate, constant product quality produce method of bio-diesel oil with the peracid value waste oil.
In order to solve the problems of the technologies described above, the present invention has adopted following technical scheme:
A kind ofly produce method of bio-diesel oil with the peracid value waste oil, high acid value waste animal and vegetable oil is carried out following steps: a. hydrolysis generates lipid acid; B. separate, isolate moisture lipid acid; C. dehydration is with moisture lipid acid dehydration; D. esterification is carried out esterification with methyl alcohol; E. flash distillation obtains biofuel (fatty acid methyl ester) through the flash distillation separating methanol.
Further, after the flash distillation of step e, also comprise step f, rectifying.
The hydrolysis temperature of described step a is 160 ℃～190 ℃, pressure 1.0MPa～1.6MPa.
The hydrolysis reaction rate is more than 98% among the described step a.Promptly generate fatty acid content and reach 98% croude fatty acids
Dewater among the described step c to moisture content below 3/1000ths of gross weight.
Esterification is 120 ℃～190 ℃ of temperature in the described steps d, exempts from catalyzer gas-liquid phase esterification under pressure 0.8MPa～1.2MPa.
Esterification to acid value drops to below 0.8 in the described steps d.
Another object of the present invention is to provide a kind of to produce the equipment of biofuel with the peracid value waste oil, and the biofuel that this equipment is produced has the yield rate height, the characteristics of constant product quality.Its technical scheme is following:
A kind ofly produce the equipment of biofuel, comprising with the peracid value waste oil:
Hydrolysis tower, steam is inserted in the bottom of hydrolysis tower, makes the reaction that in tower, is hydrolyzed of high acid value waste animal and vegetable oil;
The decompression slurry tank, the hydrolysis resultant in the hydrolysis tower is isolated swill and the moisture lipid acid that contains non-lipid impurity and glycerine in the decompression slurry tank;
The flash-evaporation dehydration tower, isolated moisture lipid acid dewaters in flashing tower;
Esterification column, lipid acid after the dehydration and methyl alcohol carry out esterification in esterification column;
The flash distillation dealcoholize column, the esterification reaction product thing is sloughed methyl alcohol in the flash distillation dealcoholize column, get biofuel.
Compared with prior art, beneficial effect of the present invention is: entire reaction course exempts to use catalyzer, need not wash, and the table of equipment number of packages obviously reduces, and reaction, separating step is few, and waste water, exhaust gas emission are few, constant product quality.
Description of drawings
Fig. 1 is a process flow diagram of the present invention;
Fig. 2 is the structural representation of equipment.
Embodiment
Below in conjunction with accompanying drawing and specific embodiment the present invention is described in further detail, but not as to qualification of the present invention.
Shown in accompanying drawing 1, Fig. 1 is a process flow diagram of the present invention, a kind ofly produces method of bio-diesel oil with the peracid value waste oil, comprises the steps:
1, hydrolysis, separation and dehydration
The purpose of this workshop section is to mix through glycerine and non-lipid that hydrolysis is removed in the raw material; Adopt the catalyst-free band to press the intermittent type hydrolysis, pretreated raw oil gets into hydrolysis tower through heating; In temperature is 160 ℃～190 ℃, and pressure is to be hydrolyzed under the condition of 1.0MPa～1.6MPa, generates croude fatty acids and glycerine; After hydrolysis is accomplished, get into the decompression slurry tank and carry out the natural gravity sedimentation, non-lipid impurity and glycerine are water-soluble; Non-lipid impurity and glycerol liquor in the gravity settling separation grease, moisture croude fatty acids get into the flash-evaporation dehydration tower and carry out flash-evaporation dehydration.
2, esterification:
Croude fatty acids after the dehydration is pressed into the filler esterification column of 316L material, 120 ℃～190 ℃ of temperature, carries out esterification under the condition of pressure 0.8MPa～1.2MPa; The overheated high speed methanol gas that has certain pressure; Directly in oil reservoir, carry out the vapour-liquid phase reaction, owing to be in the subcritical state of methyl alcohol, can be without catalyzer; Cat head is constantly discharged aqueous methanol simultaneously, impels reaction to be linear positive dirction operation.Through reaction in 4～8 hours, acid value was reduced to 0.8 following stopped reaction, is coarse biodiesel (fatty acid methyl ester) after the flash distillation dealcoholysis.
3, Methanol Recovery rectifying:
The aqueous methanol of collecting in aqueous methanol of collecting after the fatty acid methyl ester process flash distillation that generates and the miscellaneous equipment gets into the refining recycling of refining methanol system, reduces production costs.
4, rectifying:
Promptly arrive after coarse biodiesel (fatty acid methyl ester) rectifying separation refined biometric diesel oil.
5, post-processed:
Add inhibitor.The biofuel that above-mentioned raw materials is produced, oxidation stability is relatively poor, and in order to prolong the shelf lives of biofuel, the oxidation inhibitor that the later stage is added trace is very necessary, to reach GB.
Shown in accompanying drawing 2, Fig. 2 is the structural representation of equipment of the present invention.A kind ofly produce the equipment of biofuel, mainly comprise following equipment with the peracid value waste oil:
Hydrolysis tower 1, head tank 2, technology water pot 3, input and output material pump 4, decompression slurry tank 5; Flash-evaporation dehydration tower 6, esterification column 7, esterification column filler 8, recycle pump 9, recirculation heater 10, first-class heat exchanger 11, secondary condenser 12, methanol gas producer 13, methyl alcohol metering feeding pump 14, refined methanol storage tank 15, thick methyl alcohol storage tank 16, flash distillation dealcoholize column 17, open steam valve 18, emptying reducing valve 19, dehydration fresh feed pump 20.
The technology of using this equipment to produce biofuel with the peracid value waste oil is following:
Raw oil, process water be by head tank 2 and technology water pot 3, and respectively with certain proportion, quantitatively be pressed into hydrolysis tower 1, hydrolysis tower 1 bottom feeds the open steam reaction that is hydrolyzed through fresh feed pump 4; The emptying reducing valve 19 on adjustment open steam valve 18 and hydrolysis tower 1 top; Make to keep boiling state in the tower but flooding not, and keep certain pressure and temperature, after percent hydrolysis reaches 98%; Close above-mentioned valve; Open input and output material pump 4 and get into decompression slurry tanks 5 and isolate swill and moisture lipid acid, moisture lipid acid is squeezed into flash-evaporation dehydration tower 6 with the fresh feed pump 20 that dewaters and is carried out flash-evaporation dehydration, obtains water cut less than 3/1000ths croude fatty acids.
Croude fatty acids is pressed into the esterification column 7 that is added with filler 8 with recycle pump 9, and metering methanol feeding pump 14 is quantitatively squeezed into methyl alcohol continuously from refined methanol jar 15; Methyl alcohol warp interchanger 11 and methanol gas producer 13 become overheated methanol vapor and get into esterification column 7 bottoms, carry out gas-liquid esterification mutually with croude fatty acids; 10 heating of ON cycle pump 9 heater vias circulate to guarantee the temperature required and pressure of reaction simultaneously, and water and excessive methanol that reaction generates are discharged from cat head with gaseous state continuously; Be beneficial to reaction forward and carry out, be cooled to liquid, get into thick methanol tank 16 through an interchanger 11 and No. two condensing surfaces 12; Thick methyl alcohol is used for esterification once more after rectifying; When the reaction system acid value is reduced to below 0.8, stopped reaction, material is squeezed into flash distillation dealcoholize column 17 with recycle pump 9 and is removed the residual methanol in the material; Material after the dealcoholysis is called thick methyl esters, and thick methyl esters becomes through rectifying and post-processed and is biofuel.
Above embodiment is merely exemplary embodiment of the present invention, is not used in restriction the present invention, and protection scope of the present invention is defined by the claims.Those skilled in the art can make various modifications or be equal to replacement the present invention in essence of the present invention and protection domain, this modification or be equal to replacement and also should be regarded as dropping in protection scope of the present invention.
Claims (9)
1. produce method of bio-diesel oil with the peracid value waste oil for one kind, it is characterized in that, high acid value waste animal and vegetable oil is carried out following steps:
A. hydrolysis generates lipid acid;
B. separate, isolate the swill and the moisture lipid acid that contain non-lipid impurity and glycerine;
C. dehydration is with moisture lipid acid dehydration;
D. esterification is carried out esterification with methyl alcohol;
E. flash distillation obtains biofuel through the flash distillation separating methanol.
2. according to claim 1ly produce method of bio-diesel oil, it is characterized in that, after the flash distillation of step e, also comprise step f, rectifying with the peracid value waste oil.
3. according to claim 1ly produce method of bio-diesel oil, it is characterized in that the hydrolysis temperature of described step a is 160 ℃～190 ℃, pressure 1.0MPa～1.6MPa with the peracid value waste oil.
4. according to claim 1ly produce method of bio-diesel oil, it is characterized in that the hydrolysis reaction rate is more than 98% among the described step a with the peracid value waste oil.
5. according to claim 1ly produce method of bio-diesel oil, it is characterized in that with the peracid value waste oil, dewater among the described step c to moisture content below 3/1000ths of gross weight.
6. according to claim 1ly produce method of bio-diesel oil, it is characterized in that esterification is 120 ℃～190 ℃ of temperature in the described steps d, exempts from catalyzer gas-liquid phase esterification under pressure 0.8MPa～1.2MPa with the peracid value waste oil.
7. according to claim 1ly produce method of bio-diesel oil, it is characterized in that esterification to acid value drops to below 0.8 in the described steps d with the peracid value waste oil.
8. according to claim 1ly produce method of bio-diesel oil with the peracid value waste oil, it is characterized in that, the natural subsidence partition method is adopted in the described separation of step b, and said swill flash concentration obtains raw glycerine and water of condensation, and water of condensation is back to hydrolysis.
9. produce the equipment of biofuel with the peracid value waste oil for one kind, it is characterized in that, comprising:
Hydrolysis tower, steam is inserted in the bottom of hydrolysis tower, makes the reaction that in tower, is hydrolyzed of high acid value waste animal and vegetable oil;
The decompression slurry tank, the hydrolysis resultant in the hydrolysis tower is isolated swill and the moisture lipid acid that contains non-lipid impurity and glycerine in the decompression slurry tank;
The flash-evaporation dehydration tower, isolated moisture lipid acid dewaters in flashing tower;
Esterification column, lipid acid after the dehydration and methyl alcohol carry out esterification in esterification column;
The flash distillation dealcoholize column, the esterification reaction product thing is sloughed methyl alcohol in the flash distillation dealcoholize column, get biofuel.
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| CN2010102712962A CN102382716A (en) | 2010-09-03 | 2010-09-03 | Method and equipment for preparing biodiesel with high-acid-value waste oil |
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| CN2010102712962A CN102382716A (en) | 2010-09-03 | 2010-09-03 | Method and equipment for preparing biodiesel with high-acid-value waste oil |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242966A (en) * | 2013-05-20 | 2013-08-14 | 阳谷县凯歌新能源生物科技有限公司 | Technology process for producing biodiesel and key preparation device |
| CN103254996A (en) * | 2013-05-29 | 2013-08-21 | 深圳市腾浪再生资源发展有限公司 | Method and esterification tower for manufacturing biodiesel by employing gas phase alcoholysis method by utilizing waste oil |
| CN103374463A (en) * | 2012-04-26 | 2013-10-30 | 中国石油化工股份有限公司 | Preparation method of biodiesel |
| CN104086412A (en) * | 2014-06-30 | 2014-10-08 | 海盐县精细化工有限公司 | Process method for producing butyl oleate by using rape oil fatty acid |
| CN104342215A (en) * | 2013-08-05 | 2015-02-11 | 上海顶源石油化工有限公司 | Method for preparing biodiesel with alcoholysis one-step method |
| CN104419526A (en) * | 2013-09-02 | 2015-03-18 | 河南隆正生物能源有限公司 | Device for producing biodiesel from waste catering oil |
| CN107099325A (en) * | 2016-02-22 | 2017-08-29 | 中国石油化工股份有限公司 | A kind of method of sump oil desalting and dewatering |
| CN109097085A (en) * | 2017-06-20 | 2018-12-28 | 中国石油化工股份有限公司 | The pretreated method of coal tar |
| CN112159727A (en) * | 2020-09-09 | 2021-01-01 | 湖北天基生物能源科技发展有限公司 | Esterification method of waste oil |
| CN113061457A (en) * | 2021-03-10 | 2021-07-02 | 河北隆海生物能源股份有限公司 | Process and equipment for directly producing aviation kerosene by using waste oil |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1473907A (en) * | 2002-08-07 | 2004-02-11 | 四川古杉油脂化学有限公司 | Process for producing biological diesel oil |
| CN1743416A (en) * | 2004-08-30 | 2006-03-08 | 中油双星生物柴油有限公司 | Apparatus for producing biodiesel for vehicle and its preparing method |
| CN1827742A (en) * | 2006-04-06 | 2006-09-06 | 河南省商丘油脂化学厂 | Application of selective hydrolysis process in bio-diesel oil production |
| CN1958727A (en) * | 2006-11-21 | 2007-05-09 | 杨锦梁 | Method for producing biologic diesel oil, and distillation tower |
| CN101007959A (en) * | 2007-01-26 | 2007-08-01 | 河南省商丘油脂化学厂 | Hydrolysis reaction tower for producing bio diesel fuel |
| CN101020859A (en) * | 2007-03-16 | 2007-08-22 | 河南省商丘油脂化学厂 | Application of oil and fat flash vaporizing dewatering technique in biodiesel oil production |
| CN101195572A (en) * | 2006-12-08 | 2008-06-11 | 四川古杉油脂化学有限公司 | Method for synthesizing fatty acid methyl ester |
| CN101289628A (en) * | 2008-06-10 | 2008-10-22 | 河南星火生物能源有限公司 | Process for producing biodiesel from mixed fatty acid |
| CN101358140A (en) * | 2007-08-02 | 2009-02-04 | 姜皓 | Synthetic process of bio diesel oil and equipment |
| CN101440298A (en) * | 2008-12-09 | 2009-05-27 | 湘潭昭山油化科技有限公司 | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process |
| CN101818083A (en) * | 2010-06-02 | 2010-09-01 | 天津大学 | Method for preparing biodiesel by using chenopodium glaucum linn |
-
2010
- 2010-09-03 CN CN2010102712962A patent/CN102382716A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1473907A (en) * | 2002-08-07 | 2004-02-11 | 四川古杉油脂化学有限公司 | Process for producing biological diesel oil |
| CN1743416A (en) * | 2004-08-30 | 2006-03-08 | 中油双星生物柴油有限公司 | Apparatus for producing biodiesel for vehicle and its preparing method |
| CN1827742A (en) * | 2006-04-06 | 2006-09-06 | 河南省商丘油脂化学厂 | Application of selective hydrolysis process in bio-diesel oil production |
| CN1958727A (en) * | 2006-11-21 | 2007-05-09 | 杨锦梁 | Method for producing biologic diesel oil, and distillation tower |
| CN101195572A (en) * | 2006-12-08 | 2008-06-11 | 四川古杉油脂化学有限公司 | Method for synthesizing fatty acid methyl ester |
| CN101007959A (en) * | 2007-01-26 | 2007-08-01 | 河南省商丘油脂化学厂 | Hydrolysis reaction tower for producing bio diesel fuel |
| CN101020859A (en) * | 2007-03-16 | 2007-08-22 | 河南省商丘油脂化学厂 | Application of oil and fat flash vaporizing dewatering technique in biodiesel oil production |
| CN101358140A (en) * | 2007-08-02 | 2009-02-04 | 姜皓 | Synthetic process of bio diesel oil and equipment |
| CN101289628A (en) * | 2008-06-10 | 2008-10-22 | 河南星火生物能源有限公司 | Process for producing biodiesel from mixed fatty acid |
| CN101440298A (en) * | 2008-12-09 | 2009-05-27 | 湘潭昭山油化科技有限公司 | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process |
| CN101818083A (en) * | 2010-06-02 | 2010-09-01 | 天津大学 | Method for preparing biodiesel by using chenopodium glaucum linn |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103374463A (en) * | 2012-04-26 | 2013-10-30 | 中国石油化工股份有限公司 | Preparation method of biodiesel |
| CN103374463B (en) * | 2012-04-26 | 2014-10-29 | 中国石油化工股份有限公司 | Preparation method of biodiesel |
| CN103242966A (en) * | 2013-05-20 | 2013-08-14 | 阳谷县凯歌新能源生物科技有限公司 | Technology process for producing biodiesel and key preparation device |
| CN103254996B (en) * | 2013-05-29 | 2015-09-09 | 深圳市腾浪再生资源发展有限公司 | Waste grease is utilized to adopt gas phase alcoholysis method to manufacture method and the esterification column of biofuel |
| CN103254996A (en) * | 2013-05-29 | 2013-08-21 | 深圳市腾浪再生资源发展有限公司 | Method and esterification tower for manufacturing biodiesel by employing gas phase alcoholysis method by utilizing waste oil |
| CN104342215A (en) * | 2013-08-05 | 2015-02-11 | 上海顶源石油化工有限公司 | Method for preparing biodiesel with alcoholysis one-step method |
| CN104419526A (en) * | 2013-09-02 | 2015-03-18 | 河南隆正生物能源有限公司 | Device for producing biodiesel from waste catering oil |
| CN104086412A (en) * | 2014-06-30 | 2014-10-08 | 海盐县精细化工有限公司 | Process method for producing butyl oleate by using rape oil fatty acid |
| CN104086412B (en) * | 2014-06-30 | 2016-04-20 | 海盐县精细化工有限公司 | Produce oil with rape oil fatty acid the processing method of acid butyl ester |
| CN107099325A (en) * | 2016-02-22 | 2017-08-29 | 中国石油化工股份有限公司 | A kind of method of sump oil desalting and dewatering |
| CN107099325B (en) * | 2016-02-22 | 2019-06-14 | 中国石油化工股份有限公司 | A kind of method of sump oil desalting and dewatering |
| CN109097085A (en) * | 2017-06-20 | 2018-12-28 | 中国石油化工股份有限公司 | The pretreated method of coal tar |
| CN109097085B (en) * | 2017-06-20 | 2021-11-16 | 中国石油化工股份有限公司 | Coal tar pretreatment method |
| CN112159727A (en) * | 2020-09-09 | 2021-01-01 | 湖北天基生物能源科技发展有限公司 | Esterification method of waste oil |
| CN113061457A (en) * | 2021-03-10 | 2021-07-02 | 河北隆海生物能源股份有限公司 | Process and equipment for directly producing aviation kerosene by using waste oil |
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Application publication date: 20120321 |