CN101113361A - Method for producing biodiesel capable of being applied for industrial production - Google Patents
Method for producing biodiesel capable of being applied for industrial production Download PDFInfo
- Publication number
- CN101113361A CN101113361A CNA2006100294693A CN200610029469A CN101113361A CN 101113361 A CN101113361 A CN 101113361A CN A2006100294693 A CNA2006100294693 A CN A2006100294693A CN 200610029469 A CN200610029469 A CN 200610029469A CN 101113361 A CN101113361 A CN 101113361A
- Authority
- CN
- China
- Prior art keywords
- methyl alcohol
- reaction
- acid
- raw material
- enters
- 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.)
- Pending
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
-
- 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
- Liquid Carbonaceous Fuels (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of a bio-diesel manufacturing method. The method for manufacturing the bio-diesel that is applicable to the industrial production consists of the procedures that: a. pre-processing stage: waste oil removed of mechanical impurities is added into a raw material tank, heated and reserved after vacuum dehydration in a dehydrator; b. spiriting stage: the pre-processed raw material is pumped into a reactor, with the weight proportion of the raw material to methyl alcohol being 1: 0.15-0.35 and the weight percent of the raw material to catalyst being 1 to 3 percent and is heated to 60-75 DEG C; water produced in the reaction and the batching methyl alcohol then enters a recovery tower in gas phase, and the water is separated, while the pure methyl alcohol refluxes into the reactor for further reaction; The catalyst is removed when the reaction finishes, and the excessive methyl alcohol that is not involved in the reaction is purified in a methyl alcohol recovery tower and recollected; The produced crude methyl ester enters a precipitation tank, and then enters a distillation tower with a small amount of water removed for constant distillation under a decompressing condition, and is the finished product can be achieved after the distillation is cooled.
Description
Technical field
The present invention relates to a kind of production method technical field of biofuel.
Background technology
Minimizing year by year along with the mineral diesel storage capacity, reproducible bioenergy is all being sought by various countries, because fatty acid methyl ester is the most approaching at aspect such as combustionproperty, characteristic and mineral diesel, some index also surpasses mineral diesel, therefore, developed country such as America and Europe all to develop with the vegetables oil be the raw material production biofuel.Biofuel was succeeded in developing in Germany in 1988, with rapeseed oil production biofuel, and formally put on market in 1989, practicality through 3 years proves, use the various performance performances of B30 biofuel (30% biofuel+70% petrifaction diesel) machine good, do not subtract under the situation at power, reduced discharge of harmful gases significantly, biofuel is applied in Germany's legislation in 1991.
The U.S. begins with on a small scale with soybean oil production biofuel nineteen ninety, and is classified as clean fuel by national energy administration, apply, its existing blending ratio be biofuel 20% than petrifaction diesel 80%, be called for short the B20 biofuel.China also has the people to carry out the work in this respect, as Chinese patent application 92114795.3, is with natural fats and oils production biofuel, can't be extensive use of because of cost of material is high; That Chinese patent application CN1151433^ discloses is a kind of " being the method for the synthetic mixed fatty acid of raw material with the cotton oil distillation residues ", but because of its production technology immature, poor product quality, energy consumption is high and can't realize suitability for industrialized production.
Summary of the invention
The objective of the invention is to the deficiency at the prior art scheme, providing a kind of can reduce production costs, and is suitable for the preparation method of the biofuel of large-scale industrial production.
Technical scheme of the present invention is as follows:
A, pretreatment stage: sewer oil is entered material storaging tank after removing mechanical impurity, standby after entering water trap vacuum hydro-extraction after the heating;
B, fine wine stage: pump into reactor through pretreated raw material, raw material and methyl alcohol are 1: 0.15～0.35, catalyzer is that 1～3% (being weight ratio) cooperates, be heated to 60 ℃～75 ℃, the water that produces during reaction enters recovery tower with batching methyl alcohol with gas phase, isolate moisture, pure methyl alcohol is got back to again and is continued reaction in the reactor; Reaction is removed catalyzer when reaching terminal point, and the excessive methanol of participating in reaction is from methanol distillation column purifying and reclaiming in addition; The thick methyl esters that generates enters setting tank, enters distillation tower after removing small amount of moisture, the decompressing and continuous distillation, and overhead product is finished product after cooling, be pumped to the finished product basin.The used raw material of the present invention can be various sewer oils, also can be the edible wet goods that reclaims.
The used catalyzer of the present invention is mineral acid and organic acid mixture; Described mineral acid is: sulfuric acid, hydrochloric acid, phosphoric acid; Described organic acid is tosic acid, Witco 1298 Soft Acid, naphthene sulfonic acid or its homologue.
Can esterification of the present invention be a kind of reversible reaction, in time remove the water that generates in the reaction process, is the key that improves methyl ester conversion rate, because traditional way is to react in enamel still.Can't in time discharge generation water, reaction acquires a certain degree and just can't carry out towards the positive reaction direction, so reaction not exclusively, transformation efficiency is not high; And the structure that the present invention has adopted esterifier and methanol distillation column to fuse, the water that can remove in the reaction process at any time to be generated.Reaction is developed towards the positive reaction direction all the time, so reaction thoroughly, the ester conversion rate height can reach more than 93%; And this reactor can be more than the 20u ', is particularly suitable for industrialized production.Also just because of adopting this structure, the recyclable and not excessive methyl alcohol of participation reaction of purifying greatly reduces the consumption of methyl alcohol.
Embodiment
Be used for further describing the present invention with the test example by the following examples.
Embodiment 1:
The present invention adopts the continous vacuum dehydration, and water trap adopts the plank frame or the filling-material structure of particular design, and the vacuum forming device is water-ring pump or hydrojet vacuum pump.Owing to adopt the composite catalyst system, not only can make lipid acid change into methyl esters, also can make the neutral oil alcoholysis become the first enzyme, make product yield height; Because esterification is a reversible process, after esterification reaches requirement, must remove catalyzer earlier, carries out Methanol Recovery again.The thick methyl ester distilled feature of the present invention is to adopt decompression back continuous still battery.Thick methyl esters is preheated to about 180～230 ℃ through rising the pre-device of crossing of membrane type, enters evaporator tower again, and the evaporator tower heating is to adopt the falling film type interchanger, excessively goes bad in case material is heated, and its equipment is that steam jet vacuum pump or vapour pump are connected with water-ring pump.Must be through being cooled to below 20 ℃ after product steams, good to guarantee product color.
Utilize the main quality index of the biofuel that the inventive method produces as follows:
| Sequence number | Index name | Unit | Desired value |
| Superfine | |||
| 1 | Colourity | Number | ≤1 |
| 2 | Sulphur content | ％(m/m) | ≤0.05 |
| 3 | Acid number | KOH/100mJ | ≤45 |
| 4 | Ash content | ％(m/m) | ≤0.005 |
| 5 | Condensation point | ℃ | ≤-5 |
| 6 | Cold filter clogging temperature | DC | ≤-1 |
| 7 | Flash-point (remaining silent) | ℃ | ≥70 |
| 8 | 10% steams the excess carbon residue | ％(m/m) | ≤0.5 |
| 9 | Copper corrosion (5012) | Level | ≤1 |
| 10 | Moisture | ％(m/m) | Vestige |
| 11 | Mechanical impurity | Do not have | |
| 12 | Kinematic viscosity (2012) | mms | 3.6～8.0 |
| 13 | Cetane value | ＞-46 |
Claims (2)
1. production method that can be used for industrial biofuel, this method comprises the steps:
A, pretreatment stage: sewer oil is entered material storaging tank after removing mechanical impurity, standby after entering water trap vacuum hydro-extraction after the heating;
B, fine wine stage: pump into reactor through pretreated raw material, raw material and methyl alcohol are 1: 0.15～0.35, catalyzer is that 1～3% (being weight ratio) cooperates, be heated to 60 ℃～75 ℃, the water that produces during reaction enters recovery tower with batching methyl alcohol with gas phase, isolate moisture, pure methyl alcohol is got back to again and is continued reaction in the reactor; Reaction is removed catalyzer when reaching terminal point, and the excessive methanol of participating in reaction is from methanol distillation column purifying and reclaiming in addition; The thick methyl esters that generates enters setting tank, enters distillation tower after removing small amount of moisture, the decompressing and continuous distillation, and overhead product is finished product after cooling, be pumped to the finished product basin.
2. the production method that can be used for industrial biofuel as claimed in claim 1,, it is characterized in that: used catalyzer is mineral acid and organic acid mixture, and described mineral acid is sulfuric acid, hydrochloric acid or phosphoric acid; Described organic acid is tosic acid, Witco 1298 Soft Acid, naphthene sulfonic acid or its homologue.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100294693A CN101113361A (en) | 2006-07-27 | 2006-07-27 | Method for producing biodiesel capable of being applied for industrial production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100294693A CN101113361A (en) | 2006-07-27 | 2006-07-27 | Method for producing biodiesel capable of being applied for industrial production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101113361A true CN101113361A (en) | 2008-01-30 |
Family
ID=39021893
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2006100294693A Pending CN101113361A (en) | 2006-07-27 | 2006-07-27 | Method for producing biodiesel capable of being applied for industrial production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101113361A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955850A (en) * | 2010-09-28 | 2011-01-26 | 上海绿铭环保科技股份有限公司 | Complex acid catalyst for producing biodiesel from acidified oil and production method of biodiesel |
| CN102559380A (en) * | 2011-09-26 | 2012-07-11 | 中国海洋石油总公司 | Method and system for refining biodiesel crude product |
| CN103382416A (en) * | 2013-01-14 | 2013-11-06 | 江苏卡特新能源有限公司 | Biodiesel esterification reaction technology |
| CN103710155A (en) * | 2013-12-13 | 2014-04-09 | 中国林业科学研究院林产化学工业研究所 | Method for preparing biodiesel through high-temperature esterification reaction of high acid value oil |
| CN101624534B (en) * | 2008-07-12 | 2014-06-25 | 程文波 | Methanol esterification method in production of biodiesel |
| CN106378197A (en) * | 2016-08-31 | 2017-02-08 | 防城港市中能生物能源投资有限公司 | Biodiesel esterification compound acid catalyst |
-
2006
- 2006-07-27 CN CNA2006100294693A patent/CN101113361A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101624534B (en) * | 2008-07-12 | 2014-06-25 | 程文波 | Methanol esterification method in production of biodiesel |
| CN101955850A (en) * | 2010-09-28 | 2011-01-26 | 上海绿铭环保科技股份有限公司 | Complex acid catalyst for producing biodiesel from acidified oil and production method of biodiesel |
| CN102559380A (en) * | 2011-09-26 | 2012-07-11 | 中国海洋石油总公司 | Method and system for refining biodiesel crude product |
| CN103382416A (en) * | 2013-01-14 | 2013-11-06 | 江苏卡特新能源有限公司 | Biodiesel esterification reaction technology |
| CN103382416B (en) * | 2013-01-14 | 2015-12-23 | 江苏悦达卡特新能源有限公司 | A kind of technique of biodiesel esterification |
| CN103710155A (en) * | 2013-12-13 | 2014-04-09 | 中国林业科学研究院林产化学工业研究所 | Method for preparing biodiesel through high-temperature esterification reaction of high acid value oil |
| CN103710155B (en) * | 2013-12-13 | 2015-11-25 | 中国林业科学研究院林产化学工业研究所 | The method of biofuel is prepared in a kind of high-acid value grease high temperature esterification reaction |
| CN106378197A (en) * | 2016-08-31 | 2017-02-08 | 防城港市中能生物能源投资有限公司 | Biodiesel esterification compound acid catalyst |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1197937C (en) | Process for producing biological diesel oil | |
| CN101067091B (en) | Solid catalysis process of preparing biodiesel oil continuously with high acid value material | |
| CN100335594C (en) | Method for preparing biological diesel oil | |
| CN101195572A (en) | Method for synthesizing fatty acid methyl ester | |
| US20100331558A1 (en) | Method for producing fatty acid methyl ester | |
| EP2049461B1 (en) | Process for the production of biodiesel | |
| WO2007058485A1 (en) | A method for producing biodiesel using supercritical alcohols | |
| CN101113361A (en) | Method for producing biodiesel capable of being applied for industrial production | |
| CN101215233B (en) | Technique for producing fatty acid methyl ester | |
| CN1556174A (en) | Production method of biodiesel oil using high acid ralue animal and vegetable grease | |
| CN1687312A (en) | Method for producing biologic diesel oil through waterpower cavitation | |
| CN101747182A (en) | Low acid value esterification novel process | |
| CN101440298A (en) | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process | |
| CN112175744A (en) | Method for preparing biodiesel from high-acid-value kitchen waste grease | |
| CN201330241Y (en) | Device for producing refined biodiesel with high acid value oil | |
| CN101289628A (en) | Process for producing biodiesel from mixed fatty acid | |
| KR100398810B1 (en) | Method for making vegetable fuel for an internal-combustion engine | |
| CN101486923A (en) | Environment friendly process for biodiesel | |
| CN101440299A (en) | Method for preparing -10 DEC C biodiesel from waste lipid by distillation process | |
| CN102242016A (en) | Method for producing biodiesel with palm fatty acid | |
| CN101063040B (en) | Method for preparing biological diesel by hogwash oil | |
| CN103497842A (en) | New method of utilizing methanol and ethanol as ester exchange agent for preparing biodiesel | |
| TWI387646B (en) | Reverse flow esterification reactor for producing biomass diesel and its | |
| CN109135844B (en) | Preparation method of environment-friendly gasoline | |
| CN101113357A (en) | Method for producing biodiesel by quick catalysis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20080130 |