CN101168682A - Preparation method for biological diesel oil - Google Patents
Preparation method for biological diesel oil Download PDFInfo
- Publication number
- CN101168682A CN101168682A CNA2007101909308A CN200710190930A CN101168682A CN 101168682 A CN101168682 A CN 101168682A CN A2007101909308 A CNA2007101909308 A CN A2007101909308A CN 200710190930 A CN200710190930 A CN 200710190930A CN 101168682 A CN101168682 A CN 101168682A
- Authority
- CN
- China
- Prior art keywords
- oil
- exchange resin
- trickle bed
- catalyst
- anionite
- 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.)
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Links
- 239000002283 diesel fuel Substances 0.000 title abstract description 5
- 238000002360 preparation method Methods 0.000 title abstract description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 105
- 238000000034 method Methods 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 14
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 9
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 9
- 239000003921 oil Substances 0.000 claims description 23
- 235000019198 oils Nutrition 0.000 claims description 23
- 239000002551 biofuel Substances 0.000 claims description 20
- 239000011347 resin Substances 0.000 claims description 19
- 229920005989 resin Polymers 0.000 claims description 19
- 239000010773 plant oil Substances 0.000 claims description 9
- 125000003011 styrenyl group Chemical class [H]\C(*)=C(/[H])C1=C([H])C([H])=C([H])C([H])=C1[H] 0.000 claims description 8
- 239000003225 biodiesel Substances 0.000 claims description 7
- 235000013311 vegetables Nutrition 0.000 claims description 6
- 235000019484 Rapeseed oil Nutrition 0.000 claims description 5
- 239000004744 fabric Substances 0.000 claims description 5
- 235000019387 fatty acid methyl ester Nutrition 0.000 claims description 5
- 235000012424 soybean oil Nutrition 0.000 claims description 5
- 239000003549 soybean oil Substances 0.000 claims description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- 235000019483 Peanut oil Nutrition 0.000 claims description 3
- 239000004411 aluminium Substances 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- 239000000312 peanut oil Substances 0.000 claims description 3
- 125000001453 quaternary ammonium group Chemical group 0.000 claims description 3
- 235000020238 sunflower seed Nutrition 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- ZEMPKEQAKRGZGQ-AAKVHIHISA-N 2,3-bis[[(z)-12-hydroxyoctadec-9-enoyl]oxy]propyl (z)-12-hydroxyoctadec-9-enoate Chemical compound CCCCCCC(O)C\C=C/CCCCCCCC(=O)OCC(OC(=O)CCCCCCC\C=C/CC(O)CCCCCC)COC(=O)CCCCCCC\C=C/CC(O)CCCCCC ZEMPKEQAKRGZGQ-AAKVHIHISA-N 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 239000007788 liquid Substances 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 2
- 235000015112 vegetable and seed oil Nutrition 0.000 abstract 4
- 239000008158 vegetable oil Substances 0.000 abstract 4
- 238000004821 distillation Methods 0.000 abstract 1
- 238000002156 mixing Methods 0.000 abstract 1
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 24
- 235000011187 glycerol Nutrition 0.000 description 12
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000006136 alcoholysis reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 239000004793 Polystyrene Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 229920002223 polystyrene Polymers 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000006353 environmental stress Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Landscapes
- Fats And Perfumes (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
The invention discloses a method for the biological diesel oil preparation by using anion exchange resin catalyzing vegetable oil, and the method is characterized in that catalyst is packaged in small packets to be filled into a trickle bed reactor to form a catalyst bed layer, methanol steam is accessed into the bottom part of the trickle bed, after the catalyst bed layer is heated to be 65 to 100 DEG C, vegetable oil is accessed from the top part of the trickle bed, and the residence time of the vegetable oil in the trickle bed is controlled for 100 to 300 min, thereby biological diesel oil is obtained through performing distillation reseparation on the reaction product obtained. The invention adopts gas-liquid mass transfer, and the mass transfer effect is good, thereby the working procedure of continuous blending and the energy consumption needed in the traditional method can be avoided; the invention adopts the anion exchange resin catalyzing vegetable oil as the catalyst, thereby avoiding the subsequent working procedures of catalyst separating, etc., and simultaneously avoiding a great amount of waste water generated when the basic catalyst is neutralized; the anion exchange resin can be reused, and the cost is reduced; the invention adopts the trickle bed reactor to produce the biological diesel oil, and is suitable for the continuous and large scaled production.
Description
Technical field
The present invention relates to environment protection, field of renewable energy technology, be specifically related to a kind ofly prepare method of bio-diesel oil in trickle bed neutral and alkali resin catalysis grease alcoholysis reaction.
Background technology
Biofuel is the renewable energy source of cleaning, and it is to be the liquid fuel that raw material is made with animal-plant oil etc., is fine oil, diesel oil substitute.Biofuel is typical " green energy resource ", greatly develops biofuel to advancing energy substitution, reduces urban atmospheric pollution, and the Sustainable development aspect of alleviating society, economy and environment such as environmental stress has the important strategic meaning.
The preparation of biofuel at present mainly contains acid system and alkaline process homogeneous catalytic reaction.The acid system catalysis for preparing biodiesel oil is higher to the corrodibility of equipment.Generally in the industrial production adopt alkaline process catalysis, promptly oil plant and methyl alcohol prepare biofuel carrying out alcoholysis reaction intermittence in the stirring tank under the katalysis of NaOH or KOH.But also there are many shortcomings in this method: stirred-tank reactor is liquid, liquid two phase reaction, and methyl alcohol and oil plant are immiscible, needs ceaselessly to stir in reaction process, and energy consumption is big; The reaction mass transfer effect is undesirable, and can not continuous production; Reaction back homogeneous phase alkali can't reclaim, and production cost is higher; Catalyzer need neutralize, wash, and can produce a large amount of industrial wastewater pollution environment in this process.
Summary of the invention
The objective of the invention is to deficiency and defective, a kind of production method of bio-diesel oil is provided at above existing production technique.In trickle-bed reactor, as catalyzer, be under 65-100 ℃ with anionite-exchange resin in temperature, vegetables oil and methyl alcohol carry out the alcoholysis reaction of gas-liquid mass transfer, generate fatty acid methyl ester, i.e. biofuel.
Purpose of the present invention is achieved by following measure:
A kind of preparation method of bio-diesel oil, it is characterized in that catalyst pack is dressed up parcel inserts trickle-bed reactor formation beds, feed methanol steam from trickle bed bottom, beds be heated to after temperature is 65-100 ℃, again from the trickle bed top with 50-400mL/m
2The flow velocity of min feeds vegetables oil, and the residence time of controlling plant oil in trickle bed is 100-300min, and methanol steam keeps excessive therebetween, gained reaction product standing demix after distilling, and separation obtains fatty acid methyl ester and is biofuel.
Above-mentioned vegetables oil is one or more mixtures in soybean oil, genetically engineered soybean oil, rapeseed oil, transgenosis rapeseed oil, Viscotrol C, plam oil, Oleum Verniciae fordii, peanut oil, sunflower seed oil, the edible waste oil.
Above-mentioned catalyzer is an anionite-exchange resin.
Above-mentioned anionite-exchange resin can be strongly basic anion exchange resin.
Above-mentioned strongly basic anion exchange resin can be 201 macroporous strong basic styrene series anionite-exchange resin, 203 macroporous strong basic styrene series II type anionite-exchange resin, the difunctional anionite-exchange resin of 320 macroporous strong basic styrene series or 717 strong alkaline quaternary ammonium I type anionite-exchange resin (being commercially available).
The present invention adopts wire cloth that catalyst pack is dressed up parcel, and used wire cloth can be woven wire, wire netting, aluminium wire netting or copper wire gauze.
This production technique specifically can be operated as follows:
The wire cloth of catalyzer about with 50～60 orders is packaged into 1～5 * 3～300cm long strip shape parcel to be inserted in the trickle-bed reactor, feed methanol steam from the trickle bed bottom, beds is heated to after temperature is 65～100 ℃, again from the trickle bed top with 50～400mL/m
2The flow velocity of min feeds vegetables oil, and the residence time of controlling plant oil in trickle bed is 100～300min, and methanol steam keeps excessive therebetween, and unnecessary methyl alcohol is reclaimed by the reactor head condensation.Reaction product is fatty acid methyl ester and glycerine, distills out standing demix behind the methyl alcohol unnecessary in the product, and the glycerine that separates lower floor obtains fatty acid methyl ester and is biofuel.
The present invention adopts its content of gas chromatography determination and calculates productive rate.
The present invention compared with prior art has following advantage:
1. the present invention adopts anionite-exchange resin as catalyzer, avoided subsequent handlings such as catalyst separating, avoided simultaneously in the basic catalyst and the time a large amount of waste water of being produced, belong to environmentally friendly technology;
2. the present invention adopts anionite-exchange resin as catalyzer, can use repeatedly, has reduced production cost;
3. the present invention is according to the characteristic of terrestrial attraction effect and gas, adopts liquid, the circulation of vital energy in the wrong direction to spread matter, and mass transfer effect is good, avoided not stopping in the traditional method production process that stirs and required energy consumption;
4. the present invention adopts trickle-bed reactor production biofuel, is suitable for continuous, large-scale industrial production.
Embodiment
The invention will be further described by the following examples, but to the present invention without limits.
Embodiment 1
With 60 order woven wires 201 macroporous strong basic polystyrene series anion exchange resins being packaged into 3 * 140cm long strip shape parcel inserts in the trickle-bed reactor, feed methanol steam from the trickle bed bottom, after making beds be heated to 65 ℃ of methyl alcohol vaporization temperatures, again from the trickle bed top with 150mL/m
2The flow velocity of min feeds rapeseed oil, the residence time of controlling plant oil in trickle bed is 160min, methanol steam keeps excessive therebetween, unnecessary methyl alcohol is reclaimed by the reactor head condensation, reaction product is biofuel and glycerine, distill out standing demix behind the methyl alcohol unnecessary in the product, the glycerine that separates lower floor obtains biofuel, and its productive rate is 96.87%.
Embodiment 2
With 50 order woven wires 203 macroporous strong basic styrene series II type anionite-exchange resin being packaged into 1 * 200cm long strip shape parcel inserts in the trickle-bed reactor, feed methanol steam from the trickle bed bottom, the control catalyst bed temperature is 100 ℃, again from the trickle bed top with 50mL/m
2The flow velocity of min feeds soybean oil, the residence time of controlling plant oil in trickle bed is 200min, methanol steam keeps excessive therebetween, unnecessary methyl alcohol is reclaimed by the reactor head condensation, reaction product is biofuel and glycerine, distill out standing demix behind the methyl alcohol unnecessary in the product, the glycerine that separates lower floor obtains biofuel, and its productive rate is 93.20%.
Embodiment 3
With 60 order copper wire gauze the difunctional anionite-exchange resin of 320 macroporous strong basic styrene series being packaged into 4 * 4cm long strip shape parcel inserts in the trickle-bed reactor, feed methanol steam from the trickle bed bottom, the control catalyst bed temperature is 80 ℃, again from the trickle bed top with 400mL/m
2The flow velocity of min feeds peanut oil, the residence time of controlling plant oil in trickle bed is 100min, methanol steam keeps excessive therebetween, unnecessary methyl alcohol is reclaimed by the reactor head condensation, reaction product is biofuel and glycerine, distill out standing demix behind the methyl alcohol unnecessary in the product, the glycerine that separates lower floor obtains biofuel, and its productive rate is 58.26%.
Embodiment 4
With 60 order aluminium wire nettings 717 strong alkaline quaternary ammonium I type anionite-exchange resin being packaged into 3 * 7cm long strip shape parcel inserts in the trickle-bed reactor, feed methanol steam from the trickle bed bottom, after making beds be heated to 65 ℃ of methyl alcohol vaporization temperatures, again from the trickle bed top with 150mL/m
2The flow velocity of min feeds edible waste oil, the residence time of controlling plant oil in trickle bed is 250min, methanol steam keeps excessive therebetween, unnecessary methyl alcohol is reclaimed by the reactor head condensation, reaction product is biofuel and glycerine, distill out standing demix behind the methyl alcohol unnecessary in the product, the glycerine that separates lower floor obtains biofuel, and its productive rate is 73.23%.
Embodiment 5
With 60 order wire nettings 201 macroporous strong basic polystyrene series anion exchange resins being packaged into 3 * 300cm long strip shape parcel inserts in the trickle-bed reactor, feed methanol steam from the trickle bed bottom, after making beds be heated to 65 ℃ of methyl alcohol vaporization temperatures, again from the trickle bed top with 150mL/m
2The flow velocity of min feeds sunflower seed oil, the residence time of controlling plant oil in trickle bed is 160min, methanol steam keeps excessive therebetween, unnecessary methyl alcohol is reclaimed by the reactor head condensation, reaction product is biofuel and glycerine, distill out standing demix behind the methyl alcohol unnecessary in the product, the glycerine that separates lower floor obtains biofuel, and biodiesel production rate is 95.21%.
Claims (7)
1. one kind prepares method of bio-diesel oil, it is characterized in that catalyst pack is dressed up parcel inserts trickle-bed reactor formation beds, feed methanol steam from trickle bed bottom, beds be heated to after temperature is 65-100 ℃, again from the trickle bed top with 50-400mL/m
2The flow velocity of min feeds vegetables oil, and the residence time of controlling plant oil in trickle bed is 100-300min, and methanol steam keeps excessive therebetween, gained reaction product standing demix after distilling, and separation obtains fatty acid methyl ester and is biofuel.
2. method according to claim 1 is characterized in that described vegetables oil is one or more mixtures in soybean oil, genetically engineered soybean oil, rapeseed oil, transgenosis rapeseed oil, Viscotrol C, plam oil, Oleum Verniciae fordii, peanut oil, sunflower seed oil, the edible waste oil.
3. method according to claim 1 is characterized in that described catalyzer is an anionite-exchange resin.
4. method according to claim 3 is characterized in that described anionite-exchange resin is strongly basic anion exchange resin.
5. method according to claim 4 is characterized in that described strongly basic anion exchange resin is 201 macroporous strong basic styrene series anionite-exchange resin, 203 macroporous strong basic styrene series II type anionite-exchange resin, the difunctional anionite-exchange resin of 320 macroporous strong basic styrene series or 717 strong alkaline quaternary ammonium I type anionite-exchange resin.
6. method according to claim 1 is characterized in that adopting wire cloth that catalyst pack is dressed up parcel.
7. method according to claim 6 is characterized in that described wire cloth is woven wire, wire netting, aluminium wire netting or copper wire gauze.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101909308A CN101168682A (en) | 2007-12-03 | 2007-12-03 | Preparation method for biological diesel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101909308A CN101168682A (en) | 2007-12-03 | 2007-12-03 | Preparation method for biological diesel oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101168682A true CN101168682A (en) | 2008-04-30 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007101909308A Pending CN101168682A (en) | 2007-12-03 | 2007-12-03 | Preparation method for biological diesel oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101168682A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101654624A (en) * | 2008-08-21 | 2010-02-24 | 庞汝瑞 | Gaseous phase circulation production method for biodiesel and device therefor |
| CN102191135A (en) * | 2011-04-12 | 2011-09-21 | 南京工业大学 | Method for preparing biodiesel under catalysis of quaternary ammonium base ion exchange resin |
| CN104593158A (en) * | 2014-12-30 | 2015-05-06 | 青岛福瑞斯生物能源科技开发有限公司 | Method and device for reducing acid value fast |
| CN106365356A (en) * | 2016-10-27 | 2017-02-01 | 大连理工大学 | Method and device for treating organic pollutant in water of tetramino iron ligand catalyst-strong alkali resin compound system |
-
2007
- 2007-12-03 CN CNA2007101909308A patent/CN101168682A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101654624A (en) * | 2008-08-21 | 2010-02-24 | 庞汝瑞 | Gaseous phase circulation production method for biodiesel and device therefor |
| CN102191135A (en) * | 2011-04-12 | 2011-09-21 | 南京工业大学 | Method for preparing biodiesel under catalysis of quaternary ammonium base ion exchange resin |
| CN104593158A (en) * | 2014-12-30 | 2015-05-06 | 青岛福瑞斯生物能源科技开发有限公司 | Method and device for reducing acid value fast |
| CN106365356A (en) * | 2016-10-27 | 2017-02-01 | 大连理工大学 | Method and device for treating organic pollutant in water of tetramino iron ligand catalyst-strong alkali resin compound system |
| CN106365356B (en) * | 2016-10-27 | 2022-10-28 | 大连理工大学 | Method and device for treating organic pollutants in water by using tetra-amino iron ligand catalyst-strong basic resin composite system |
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Open date: 20080430 |