CN105087084A - Method for preparing biologic diesel oil through catalysis - Google Patents
Method for preparing biologic diesel oil through catalysis Download PDFInfo
- Publication number
- CN105087084A CN105087084A CN201410192855.9A CN201410192855A CN105087084A CN 105087084 A CN105087084 A CN 105087084A CN 201410192855 A CN201410192855 A CN 201410192855A CN 105087084 A CN105087084 A CN 105087084A
- Authority
- CN
- China
- Prior art keywords
- acid
- carboxylate
- grease
- carboxylate salt
- race
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
Landscapes
- Lubricants (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention discloses a method for preparing biologic diesel oil through catalysis. The method comprises the step of enabling fat, monohydric alcohol and carboxylate to perform a contact reaction, wherein the conditions of the contact reaction comprise that the temperature is lower than or equal to 300 DEG C, the pressure is 0.1-10MPa, and the carboxylate contains at least one kind of IV A group metal carboxylate, I B group metal carboxylate, II B group metal carboxylate, IV B group metal carboxylate, VII B group metal carboxylate, VIII group metal carboxylate and lanthanide metal carboxylate. The method disclosed by the invention can increase the yield of the biologic diesel oil. Besides, because the carboxylate is used as a catalyst, and lower temperature and pressure are matched with the catalyst, when the fat with a high acid value and a high impurity content is processed, the biologic diesel oil can also be prepared at a high yield. Besides, in the method provided by the invention, the fat does not need to be pretreated, (for example pre-esterification treatment is not needed), so that the process of preparing the biologic diesel oil is simplified, and the production efficiency is greatly improved.
Description
Technical field
The present invention relates to a kind of method of catalysis for preparing biodiesel oil.
Background technology
Biofuel is carried out transesterification reaction by grease and monohydroxy-alcohol and is obtained, and has fatty acid ester (i.e. biofuel), in addition mono-glycerides, two sweet esters, glycerine in reaction product, and unreacted alcohol and grease (i.e. triglyceride level).In prior art, the preparation method of biofuel can be divided into acid catalyzed process, base catalysis method, enzyme catalysis method and supercritical methanol technology.
CN1473907A adopts the tankage of vegetable oil refining and edible refiltered oil to be raw material, catalyzer is by mineral acids such as sulfuric acid, hydrochloric acid, tosic acid, Witco 1298 Soft Acid, naphthene sulfonic acid or organic acid is composite forms, produce through operations such as acidifying removal of impurities, continuously dehydrating, esterification, layering, underpressure distillation, the pressure of continous vacuum dehydration is 0.08-0.09MPa, temperature 60-95 DEG C, dehydration is to water-content less than 0.2%, esterif iotacation step catalyst charge 1-3%, esterification temperature 60-80 DEG C, 6 hours reaction times.Reaction after product first neutralizes removing catalyzer, and then, layering is except anhydrating, and the after product that anhydrates obtains biofuel through underpressure distillation.But acid catalyzed speed of response is slow, produces a large amount of spent acid, contaminate environment.
In method disclosed in DE3444893, with acid catalyst, normal pressure, 50-120 DEG C, carries out esterification by free fatty acids and alcohol, carries out pre-esterification process to oil plant, then under base metal catalysts, carry out transesterification reaction, but the acid catalyst left over will be neutralized by alkali, the amount of base metal catalysts can increase.Adopt pre-esterification, make work flow elongated, facility investment, energy consumption significantly rises, and in addition, basic catalyst need be removed from product, has a large amount of waste water to produce, and more difficult recovery glycerine.
In method disclosed in US5713965A, under the existence of lipase, hexane makes solvent, and grease and alcohol reaction prepare fatty acid methyl ester, i.e. diesel-fuel.
In method disclosed in CN1472280A, using fatty acid ester as acyl acceptor, under the existence of biological enzyme, catalysis biological carries out transesterification reaction production biofuel.Adopt enzyme catalyst exist deficiency be: long reaction time, efficiency are lower, and enzyme catalyst cost is higher, and in high purity methanol easy in inactivation.
JP9905431 discloses a kind of method being prepared fatty acid ester by grease and monohydroxy-alcohol reaction, the method comprises reacts to obtain fatty acid ester by methyl alcohol and grease, at 270-280 DEG C, under 11-12MPa condition, fatty acid methyl ester production rate is 55-60%, can find out, adopt the middle and high platen press of continuous print, still there is the problem that fatty acid ester yield is lower.
Summary of the invention
The present invention, in order to overcome the above-mentioned defect in the preparation method of existing biofuel, provides a kind of preparation method of new biofuel, and the method technical process is simple, and under lesser temps and pressure, improve the yield of biofuel.
To achieve these goals, the invention provides a kind of method of catalysis for preparing biodiesel oil, the method comprises makes grease, monohydroxy-alcohol and carboxylate salt contact reacts, described catalytic condition comprises: temperature≤300 DEG C, pressure is 0.1-10MPa, and described carboxylate salt is at least one in IV A race, I B race, II B race, IV B race, VII B race, VIII race and carboxylate of lanthanide metals.
Method of the present invention can improve the yield of biofuel, and, owing to using carboxylate salt as catalyzer, and coordinate lower temperature and pressure, to high acid value and the grease of high impurity content process, still can prepare biofuel by high yield.Meanwhile, in method provided by the invention, do not need to carry out pre-treatment (as pre-esterification process) to described grease, thus simplify the process of preparation biofuel, therefore, substantially increase production efficiency.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The method of catalysis for preparing biodiesel oil provided by the invention comprises makes grease, monohydroxy-alcohol and carboxylate salt contact reacts, described catalytic condition comprises: temperature≤300 DEG C, pressure is 0.1-10MPa, and described carboxylate salt is at least one in IV A race, I B race, II B race, IV B race, VII B race, VIII race and carboxylate of lanthanide metals.
In the present invention, described grease can be the grease of various routine, and its main component is fatty acid triglycercide, such as, described grease can be at least one in Vegetable oil lipoprotein, animal grease and microbial oil, can also be frying oil and/or rotten waste oil in addition.Described Vegetable oil lipoprotein such as can comprise soybean oil, rapeseed oil, peanut oil, wunflower seed oil, plam oil, Oleum Cocois and come from the material (comprising the tall oil produced in paper-making process) containing fatty group of the fruit of other various farm crop and wild plant, stem, leaf, limb and root.Animal grease such as can comprise lard, butter, sheep oil, fish oil etc.
In the present invention, described monohydroxy-alcohol can be the monohydroxy-alcohol of carbonatoms between 1-6, can be saturated alcohol, also can be unsaturated alcohol.Under preferable case, described monohydroxy-alcohol is at least one in methyl alcohol, ethanol, propyl alcohol, vinyl carbinol, butanols and amylalcohol, more preferably methyl alcohol and/or ethanol.Described propyl alcohol can be n-propyl alcohol and/or Virahol, and described butanols can be the isomer of propyl carbinol and/or propyl carbinol, and described amylalcohol can be the isomer of Pentyl alcohol and/or Pentyl alcohol.
In the present invention, as long as described grease contacts the yield that can improve biofuel with monohydroxy-alcohol with carboxylate salt in aforementioned temperature with pressure range, and there is no particular limitation for the consumption of carboxylate salt.Under preferable case, relative to the grease of 100 weight parts, the consumption of described carboxylate salt is 0.001-5 weight part.More preferably in situation, relative to the grease of 100 weight parts, the consumption of described carboxylate salt is 0.5-2 weight part.Most preferably, relative to the grease of 100 weight parts, the consumption of described carboxylate salt is 0.6-1 weight part.
In the present invention, described carboxylate salt is at least one in IV A race, I B race, II B race, IV B race, VII B race, VIII race and carboxylate of lanthanide metals.Preferably, described carboxylate salt is at least one in zinc carboxylate, ferric carboxylate, manganese carboxylate, carboxylic acid zirconium, cerium carboxylate, copper carboxylate, carboxylic acids of lead and calcium carboxylates, is more preferably at least one in zinc carboxylate, carboxylic acid zirconium and manganese carboxylate.
Described carboxylate salt can be saturated carboxylic acid salt, also can be salt unsaturated carboxylic acid, more preferably, described carboxylate salt can be the carboxylate salt of 1-30 for carbonatoms, be preferably the carboxylate salt that carbonatoms is 7-20, be more preferably the carboxylate salt that carbonatoms is 12-20, most preferably be at least one in octadecanoate (stearate), palmate (cetylate), Varicetin (oleate) and hexadecylene hydrochlorate (plam oil hydrochlorate).
According to further preferred embodiment of the present invention, described carboxylate salt is zinc octadecanate, stearic acid iron, stearic acid zirconium, stearic acid manganese, calcium stearate, palmitic acid zinc, palmitic acid iron, palmitic acid zirconium, palmitic acid manganese, palmitic acid calcium, octadecenic acid zinc, octadecenic acid iron, octadecenic acid zirconium, octadecenic acid manganese, octadecenic acid calcium, gaidic acid zinc, gaidic acid iron, gaidic acid zirconium, at least one in gaidic acid manganese and gaidic acid calcium, most preferably, described carboxylate salt is zinc octadecanate, palmitic acid zinc, stearic acid zirconium, palmitic acid zirconium, stearic acid manganese, palmitic acid manganese, octadecenic acid zinc, gaidic acid zinc, octadecenic acid zirconium, gaidic acid zirconium, at least one in octadecenic acid manganese and gaidic acid manganese.
In the present invention, when the consumption of described monohydroxy-alcohol increases, the transformation efficiency that described grease is converted into lipid acid unitary alcohol ester can be improved, thus improve the productive rate of biofuel.Consider the cost of the production process of biofuel and the yield of biofuel, the weight ratio of described grease and monohydroxy-alcohol can be 1:0.05-1, is preferably 1:0.1-0.6, is more preferably 1:0.2-0.6.
In catalytic condition, temperature is higher, and reaction conversion ratio is higher, but temperature higher than 300 DEG C time, reaction product is black, has burnt matter to produce, and meanwhile, glycerine also can be caused to decompose; Temperature is lower, can reduce again the yield of biofuel, and therefore, in foregoing temperature range, preferable temperature is 100-300 DEG C, is more preferably 100-200 DEG C.Equally, improve pressure favourable to reaction, but pressure is too high, makes the investment of device and process cost improve more, so in foregoing pressure ranges, preferred pressure is 0.1-5MPa, is more preferably 0.1-2MPa.
The preparation that described contact reacts can carry out biofuel well known by persons skilled in the art and meeting in the reactor of aforementioned temperature and pressure range is carried out, described reactor can be tubular reactor, also can be tank reactor (as autoclave).
When adopting tank reactor, described reactor, preferably with whipping appts, like this, is more conducive to the yield improving biofuel.When carrying out the contact reacts of grease, monohydroxy-alcohol and grease derivative, described grease, monohydroxy-alcohol and grease derivative can be provided to reactor separately, are provided to reactor after also can mixing.
When adopting tubular reactor, grease and monohydroxy-alcohol can be supplied to reactor separately, or be supplied to reactor by after their pre-mixings.Preferably, controlling liquid hourly space velocity is 0.1-20h-1.Before being supplied to reactor, with preheater by material preheating, also directly can enter reactor.If employing preheater, can by grease preheating together with after monohydroxy-alcohol difference preheating or mixing.In tubular reactor, grease and monohydroxy-alcohol preferably enter tubular reactor from tubular reactor bottom, and reacting coarse product flows out from tubular reactor upper end.
In a preferred embodiment, described method provided by the invention also comprises the mixture obtained after contact reacts isolates lipid acid unitary alcohol ester (mixed ester phase, containing fatty acid ester, mono-glycerides, two sweet esters and unreacted triglyceride level etc.), the method of described separation can adopt conventional separation method to implement, such as, the method for underpressure distillation can be adopted to realize.
In further preferred embodiment, described method provided by the invention isolates monohydroxy-alcohol before being also included in the mixture obtained after contact reacts and isolating lipid acid unitary alcohol ester.The method being separated monohydroxy-alcohol can adopt conventional method (as distillation) to realize.Isolated monohydroxy-alcohol can be recycled.
In preferred embodiment, before isolating lipid acid unitary alcohol ester, isolate glycerine after method provided by the invention is also included in the mixture obtained after contact reacts and isolates monohydroxy-alcohol.The method of separation of glycerin can adopt conventional method to realize, such as, can be realized by settlement separate method.Isolated glycerine can be recycled.
According to method provided by the invention, to the acid number of described grease, there is no particular limitation, such as, can be 0.1-200mgKOH/g.Method of the present invention also can prepare biofuel with higher yields when utilizing the grease of high acid value to carry out contact reacts, and therefore, the acid number of described grease can be 60-200mgKOH/g, is more preferably 90-200mgKOH/g." acid number " refers under test conditions, in and the milligram number of potassium hydroxide needed for 1g grease free fatty acid, measure according to the indicator method in GB/T5530-1998 standard.
The present invention is described in detail by the following examples.The raw material used in embodiment, unless stated otherwise, is commercially available prod.And in the examples below, the yield of biofuel is calculated by following formula:
Yield=(quality of the quality/grease of the final biofuel obtained) × 100% of biofuel.
Embodiment 1
Be the soybean oil of 0.9mgKOH/g by 100g acid number, 17g methyl alcohol and 1.7g zinc octadecanate add in autoclave together, under the condition of temperature 140 DEG C, pressure 0.7MPa and stirring velocity 200 revs/min, react 1.5 hours, obtain reacting coarse product.Reacting coarse product is distilled, at the bottom of still < 150 DEG C condition under remove methyl alcohol, and methyl alcohol is reclaimed and reuses, leftover materials are isolated glycerine mutually after, mutually underpressure distillation is carried out to the mixed ester obtained, steam material and be biofuel, the yield of biofuel is 83.9%.
Embodiment 2
Be that the rapeseed oil of 1.7mgKOH/g, 17g methyl alcohol and 1.7g zinc octadecanate add in autoclave together by 100g acid number, under the condition of temperature 140 DEG C, pressure 0.7MPa and stirring velocity 200 revs/min, react 1.5 hours, obtain reacting coarse product.Reacting coarse product is distilled, at the bottom of still < 150 DEG C condition under remove methyl alcohol, and methyl alcohol is reclaimed and reuses, leftover materials are isolated glycerine mutually after, mutually underpressure distillation is carried out to the mixed ester obtained, steam material and be biofuel, the yield of biofuel is 84.7%.
Embodiment 3
Be the waste grease of 91mgKOH/g by 100g acid number, 17g methyl alcohol and 0.7g palmitic acid zirconium add in autoclave together, under the condition of temperature 140 DEG C, pressure 0.7MPa and stirring velocity 200 revs/min, react 1.5 hours, obtain reacting coarse product.Reacting coarse product is distilled, at the bottom of still < 150 DEG C condition under remove methyl alcohol, and methyl alcohol is reclaimed and reuses, leftover materials are isolated glycerine mutually after, mutually underpressure distillation is carried out to the mixed ester obtained, steam material and be biofuel, the yield of biofuel is 92.3%.
Embodiment 4
Be the waste grease of 40mgKOH/g by 100g acid number, 17g methyl alcohol and 0.7g octadecenic acid manganese (manganese oleate) add in autoclave together, under the condition of temperature 140 DEG C, pressure 0.7MPa and stirring velocity 200 revs/min, react 1.5 hours, obtain reacting coarse product.Reacting coarse product is distilled, at the bottom of still < 150 DEG C condition under remove methyl alcohol, and methyl alcohol is reclaimed and reuses, leftover materials are isolated glycerine mutually after, mutually underpressure distillation is carried out to the mixed ester obtained, steams material and be biofuel.The yield of biofuel is 84.4%.
Embodiment 5
Be the sunflower seed oil of 0.4mgKOH/g by 100g acid number, 17g methyl alcohol and 0.9g stearic acid iron add in autoclave together, under the condition of temperature 130 DEG C, pressure 0.6MPa and stirring velocity 200 revs/min, react 2 hours, obtain reacting coarse product.Reacting coarse product is distilled, at the bottom of still < 150 DEG C condition under remove methyl alcohol, and methyl alcohol is reclaimed and reuses, leftover materials are isolated glycerine mutually after, mutually underpressure distillation is carried out to the mixed ester obtained, steam material and be biofuel, the yield of biofuel is 49.9%.
Comparative example 1
Biofuel is prepared according to the method for embodiment 5, unlike, do not add stearic acid iron, the yield of biofuel is 2.7%.
Comparative example 2
Be the sunflower seed oil of 0.4mgKOH/g by 100g acid number, 25g methyl alcohol and 4g aluminium distearate add in autoclave together, under the condition of temperature 160 DEG C, pressure 1.2MPa and stirring velocity 400 revs/min, react 4 hours, obtain reacting coarse product.Reacting coarse product is distilled, at the bottom of still < 150 DEG C condition under remove methyl alcohol, and methyl alcohol is reclaimed and reuses, leftover materials are isolated glycerine mutually after, mutually underpressure distillation is carried out to the mixed ester obtained, steam material and be biofuel, the yield of biofuel is 6%.
Embodiment 6
Take acid number as the waste grease of 7mgKOH/g be raw material, in alcohol oil quality than 0.2, under the condition of liquid hourly space velocity 1.2h-1, grease and methyl alcohol are continuously provided in tubular reactor, adding weight is the stearic acid iron of grease weight 0.15% and the palmitic acid calcium of grease weight 0.05%, controlling temperature in reactor is 260 DEG C, pressure is 6MPa, reacting coarse product is through distilling out unreacted methyl alcohol, standing separation glycerine phase, rectification under vacuum mixed ester phase, steams material and is biofuel, the yield 85.1% of biofuel.
Embodiment 7
Take acid number as the soybean oil of 0.6mgKOH/g be raw material, in alcohol oil quality than 0.2, under the condition of liquid hourly space velocity 1.2h-1, oil and methyl alcohol are continuously provided in tubular reactor, add the octadecenic acid zinc (zinc oleate) that weight is grease weight 0.2%, controlling temperature in reactor is 260 DEG C, and pressure is 6MPa, and reacting coarse product is through distilling out unreacted methyl alcohol, standing separation glycerine phase, underpressure distillation mixed ester phase, steams material and is biofuel, the yield 81% of biofuel.
As can be seen from the above embodiments, method of the present invention can significantly improve the yield of biofuel.Especially, amount and the reaction conditions of the carboxylate salt used in comparative example 2 are all better than embodiment 5, but the yield of biofuel is far below embodiment 5, illustrates and only have specific carboxylate salt in use the present invention to carry out as catalyzer the yield that contact reacts can significantly improve biofuel.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. the method for a catalysis for preparing biodiesel oil, it is characterized in that, the method comprises makes grease, monohydroxy-alcohol and carboxylate salt contact reacts, described catalytic condition comprises: temperature≤300 DEG C, pressure is 0.1-10MPa, and described carboxylate salt is at least one in IV A race, I B race, II B race, IV B race, VII B race, VIII race and carboxylate of lanthanide metals.
2. method according to claim 1, wherein, relative to the grease of 100 weight parts, the consumption of described carboxylate salt is 0.001-5 weight part.
3. method according to claim 2, wherein, relative to the grease of 100 weight parts, the consumption of described carboxylate salt is 0.5-2 weight part.
4. according to the method in claim 1-3 described in any one, wherein, described carboxylate salt is at least one in zinc carboxylate, ferric carboxylate, manganese carboxylate, carboxylic acid zirconium, cerium carboxylate, copper carboxylate, carboxylic acids of lead and calcium carboxylates.
5. according to the method in claim 1-3 described in any one, wherein, the carboxylate salt of described carboxylate salt to be carbonatoms be 1-30, is preferably the carboxylate salt that carbonatoms is 7-20, is more preferably at least one in octadecanoate, palmate, Varicetin and hexadecylene hydrochlorate.
6. method according to claim 5, wherein, described carboxylate salt is at least one in zinc octadecanate, stearic acid iron, stearic acid zirconium, stearic acid manganese, calcium stearate, palmitic acid zinc, palmitic acid iron, palmitic acid zirconium, palmitic acid manganese, palmitic acid calcium, octadecenic acid zinc, octadecenic acid iron, octadecenic acid zirconium, octadecenic acid manganese, octadecenic acid calcium, gaidic acid zinc, gaidic acid iron, gaidic acid zirconium, gaidic acid manganese and gaidic acid calcium.
7. method according to claim 1, wherein, the weight ratio of described grease and monohydroxy-alcohol is 1:0.05-1.
8. method according to claim 1, wherein, described catalytic condition comprises: temperature is 100-300 DEG C, and pressure is 0.1-5MPa.
9. the method according to claim 1 or 8, wherein, described catalytic condition comprises: temperature is 100-200 DEG C, and pressure is 0.1-2MPa.
10. method according to claim 1, wherein, the acid number of described grease is 0.1-200mgKOH/g, is preferably 60-200mgKOH/g, is more preferably 90-200mgKOH/g.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410192855.9A CN105087084B (en) | 2014-05-08 | 2014-05-08 | A kind of method of catalysis for preparing biodiesel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410192855.9A CN105087084B (en) | 2014-05-08 | 2014-05-08 | A kind of method of catalysis for preparing biodiesel oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105087084A true CN105087084A (en) | 2015-11-25 |
| CN105087084B CN105087084B (en) | 2017-09-29 |
Family
ID=54568429
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410192855.9A Active CN105087084B (en) | 2014-05-08 | 2014-05-08 | A kind of method of catalysis for preparing biodiesel oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105087084B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109423359A (en) * | 2017-08-30 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of method of stable preparation biodiesel |
| CN109971553A (en) * | 2017-12-27 | 2019-07-05 | 中国石油化工股份有限公司 | A method of improving biodiesel yield |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1923990B (en) * | 2005-08-31 | 2010-12-22 | 中国石油化工股份有限公司 | Process for preparing fatty acid ester |
| CN102337182A (en) * | 2010-07-23 | 2012-02-01 | 中国石油化工股份有限公司 | Preparation method of biodiesel |
-
2014
- 2014-05-08 CN CN201410192855.9A patent/CN105087084B/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109423359A (en) * | 2017-08-30 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of method of stable preparation biodiesel |
| CN109423359B (en) * | 2017-08-30 | 2022-03-11 | 中国石油化工股份有限公司 | Method for stably preparing biodiesel |
| CN109971553A (en) * | 2017-12-27 | 2019-07-05 | 中国石油化工股份有限公司 | A method of improving biodiesel yield |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105087084B (en) | 2017-09-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Hasheminejad et al. | Upstream and downstream strategies to economize biodiesel production | |
| US8288573B2 (en) | Process for preparing a bio-diesel | |
| CN101200648B (en) | Preparation method of biological diesel fuel | |
| US9938487B2 (en) | Method for preparing fatty acid alkyl ester using fat | |
| CN105132192A (en) | Biodiesel preparation method | |
| CN101070480A (en) | Process for preparing biological diesel oil | |
| CN105273851B (en) | A method of preparing aliphatic ester | |
| CN101200649B (en) | Preparation method of biological diesel fuel | |
| CN100548963C (en) | A kind of method for preparing fatty acid ester | |
| CN1904013A (en) | Method of lowering acid value of oil and fat | |
| CN105087084A (en) | Method for preparing biologic diesel oil through catalysis | |
| CN100460482C (en) | Method of preparing organism diesel oil from mixing plant oil | |
| CN1900224B (en) | Process for preparing biological diesel oil | |
| CN105647655B (en) | Method for preparing biodiesel | |
| CN118207045A (en) | Method for preparing fatty acid ester by adopting solid catalyst | |
| CN105087083B (en) | A method of preparing biodiesel | |
| CN109971553A (en) | A method of improving biodiesel yield | |
| US8500828B2 (en) | Process for preparing a bio-diesel | |
| CN105199857A (en) | Method for improving yield of biodiesel | |
| CN105296167A (en) | Method for preparing biodiesel through catalysis | |
| CN102337182A (en) | Preparation method of biodiesel | |
| CN105176694B (en) | A method of preparing biodiesel | |
| CN104059781B (en) | A kind of preparation method of biofuel | |
| CN109423359B (en) | Method for stably preparing biodiesel | |
| CN105861161A (en) | Preparation method of biodiesel by using solid catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |