CN200951999Y - Apparatus for producing biological diesel oil - Google Patents
Apparatus for producing biological diesel oil Download PDFInfo
- Publication number
- CN200951999Y CN200951999Y CNU2006200193433U CN200620019343U CN200951999Y CN 200951999 Y CN200951999 Y CN 200951999Y CN U2006200193433 U CNU2006200193433 U CN U2006200193433U CN 200620019343 U CN200620019343 U CN 200620019343U CN 200951999 Y CN200951999 Y CN 200951999Y
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- pipeline
- valve
- port valve
- methanol
- esterification
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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
-
- 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
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
Abstract
A device for producing biodiesel belongs to the technical field of chemical equipment, which comprises a methanol gasifier (1), an esterification/interesterification reactor (23) connected with the methanol gasifier (1) by a pipe (51) and three-way valves (8, 50, 46), a vapor generator (24) connected with the esterification/interesterification reactor (23) by a pipe (42) and a two-way valve (45), an oil-water separator (28) connected with the vapor generator (24) by an air pressure balancing passage (27), a pipe (39) and a two-way valve (38), a biodiesel collector (31) that is connected with the oil-water separator (28) by an air pressure balancing passage (30) and a biodiesel discharge port (32) and that is provided with a two-way valve (36) at the lower part thereof, and a finished biodiesel tank (34) connected with the biodiesel collector (31) by a pipe (35) and a two-way valve (33). The utility model has the advantages of compact structure, low cost, good versatility and flexibility and no environmental pollution, and is suitable for raw materials of different qualities.
Description
Technical field:
The utility model relates to a kind of preparation biofuel device, belongs to technical field of chemical.Suitable especially is the raw material production biofuel with lipid acid, oil from high acid value waste animal and plant fat and neutral grease etc.
Background technology:
Biofuel is the long-chain fat acid monoester for preparing from reproducible liquid starting material (as various animal-plant oil), it forms with petrifaction diesel quite similar, alternative petrifaction diesel, objectionable impurities is lower more than 50% than traditional petrifaction diesel in the tail gas that the burning rear engine gives off, and is a kind of novel environmental-protective and regenerative energy.Along with environment protection and exhausted two hang-ups of petroleum resources are more and more paid close attention to, biofuel has become the focus that the countries in the world new forms of energy are developed.
The production method of biofuel mainly is an ester-interchange method, and this method requires the acid number of raw material must carry out alkali refining or pre-esterification acid reduction processing in advance for high-acid-value material less than 1.0.Production unit mainly comprises alkali refining or pre-esterification device, transesterify device, water washing device, vacuum distillation apparatus etc., the whole process flow complexity, equipment used is bulky, complex structure, energy consumption are big, three wastes discharge amount is big, environmental pollution is big, and production cost is higher.And most of production units only are applicable to a kind of or a few raw material, not the tool mobility of raw material suitability and device widely.
Summary of the invention:
The purpose of this utility model is to overcome the deficiency of prior art, and a kind of collection esterification device, transesterify device, methanol gasifying device and steam distillation device are provided is one, can lipid acid, oil from high acid value waste animal and plant fat and neutral grease etc. be removable, the universal device of raw material production biofuel.
The technical solution of the utility model is:
This device is by methanol gasifying device (1), by pipeline (51) and T-valve (8), (50), (46) esterification that is connected with methanol gasifying device (1), transesterification reactor (23), by pipeline (42) and two-port valve (45) and esterification, the steam generator (24) that transesterification reactor (23) connects, by air pressure balance passage (27), the water-and-oil separator (28) that pipeline (39) and two-port valve (38) are connected with steam generator (24), by air pressure balance passage (30), the biofuel collector (31) of two-port valve (36) is equipped with in its underpart that biofuel discharge outlet (32) is connected with water-and-oil separator (28), forms by the product biofuel storage tank (34) that pipeline (35) and two-port valve (33) are connected with biofuel collector (31); Wherein:
A. the inside of methanol gasifying device (1) is provided with that the left side that well heater (2), top be provided with methanol rectification post (6), methanol gasifying device (1) is provided with the condenser (11) by T-valve (8) and pipe connection, methyl alcohol storage tank (5), the lower part outlet place that is connected with (4) and pipeline (3) by T-valve (7) is provided with connecting tube and two-port valve (52);
B. esterification, the inside of transesterification reactor (23) is provided with well heater (43), be connected and be equipped with on it methanol vapor sparger (44) of check valve (54) with methanol vapor inlet (53), be equipped with the retaining that stirs pump liquid influx (22) on it and pull (21), the top is provided with by two-port valve (17), (18), (20) and pipeline (12), (25) condenser of Lian Jieing (19), the left side at top is provided with respectively by two-port valve (9), (13), (15) and the raw oil material storage tank (10) of pipe connection, basic catalyst storage tank (14), an acidic catalyst storage tank (16), esterification, the left side of transesterification reactor (23) is provided with the stirring pump (49) with pipe connection, the by product raw glycerine storage tank (48) that is connected with pipeline and T-valve (47);
C. the inside of steam generator (24) is provided with that well heater (41), top are provided with two-port valve (26), the lower part outlet place is provided with two-port valve (40);
D. the inside of water-and-oil separator (28) is provided with by pipeline and condenser (29) banded condensate outlet (37), and the top is provided with the condenser (29) that is connected with pipeline (25).
Device of the present utility model can neutral grease be a raw material both, also can acid grease, swill wet goods catering trade waste oil or lipid acid produces thing diesel oil next life for raw material.Reactor of the present utility model also can be used for the rectifying of methyl alcohol simultaneously, reclaims the methyl alcohol in the aqueous methanol.
Advantage of the present utility model is:
1, collection esterification device, transesterify device, methanol gasifying device and steam distillation device are one, compact construction, and the utilization ratio height, cost is low.
2, material benzenemethanol form with gas in the utility model recycles, and has improved use ratio of methanol; Esterification is with water, methanol rectification and gasification organically to combine in the utility model continuously, and moisture stays in the outer methanol gasifying device of esterification main body system by rectifying device, improves the efficient of esterification, reaches the sour effect of continuously fast prompt drop.
3, adopt the steam distillation refining biodiesel, avoid traditional water washing process and underpressure distillation, can obtain highly purified product, reduced the investment of pressure-resistant equipment and the energy consumption that by-product glycerin reclaims again.
4, whole plant has versatility, is applicable to the raw material of the different qualities of various different sourcess, the animal-plant oil of promptly various lipid acid, high acid value and various neutral grease.
5, equipment has good handiness, can be made into movably small-sized or medium-sized production equipment according to the raw material supply situation, and processing ease can be realized automatization control.
6, the basic nothing " three wastes " that realizes is discharged in the production process, has environment friendly.
Description of drawings:
Fig. 1 is a structural representation of the present utility model.
Fig. 2 is the structural representation of methyl alcohol sparger (44).
Sequence number is respectively among the figure: 1-methanol gasifying device, 2-well heater, 3-pipeline, the 4-T-valve, 5-methyl alcohol storage tank, 6-methanol rectification post, the 7-T-valve, 8-T-valve, 9-two-port valve, 10-raw oil material storage tank, 11-condenser, 12-pipeline, the 13-two-port valve, 14-basic catalyst storage tank, 15-two-port valve, 16-an acidic catalyst storage tank, 17-two-port valve, 18-two-port valve, the 19-condenser, the 20-two-port valve, the 21-retaining is pulled, 22-stirs pump liquid influx, 23-esterification, transesterification reactor, the 24-steam generator, the 25-pipeline, 26-two-port valve, 27-air pressure balance passage, the 28-water-and-oil separator, 29-condenser, 30-air pressure balance passage, 31-biofuel collector, 32-biofuel discharge outlet, 33-two-port valve, 34-product biofuel storage tank, 35-pipeline, 36-two-port valve, the 37-condensate outlet, 38-two-port valve, 39-pipeline, the 40-two-port valve, 41-well heater two-port valve, 42-pipeline, the 43-well heater, 44-methanol vapor sparger, 45-two-port valve, 46-T-valve, the 47-T-valve, 48-by product raw glycerine storage tank, 49-stirs pump, 50-T-valve, the 51-pipeline, the 52-two-port valve, 53-methanol vapor inlet, 54-check valve.
Embodiment:
The utility model is described in further detail below in conjunction with accompanying drawing.
Embodiment 1: vegetable oil acid is the feedstock production biofuel
Operating process is: open two-port valve door (9), raw material in the raw material storage tank (10) is quantitatively joined in the reactor (23), start and stir pump (49), under constantly stirring, open two-port valve door (15), the methanol solution of an acidic catalyst in an acidic catalyst storage tank (16) quantitatively is added in the reactor (23), simultaneously methyl alcohol in the methyl alcohol storage tank (5) is added in the methanol gasifying reactor (1) by T-valve (4).Regulate T-valve (7 respectively, 8,46,50) and two-port valve (17,18,20,45), open well heater (2,43), the temperature that temperature in the controlling reactor (23) remains in 100 ± 5 ℃ and the reactor (1) remains on 60～70 ℃, make the material in reactor (23) and the reactor (1) form following circulation: the methanol vapor that methanol gasifying reactor (1) produces is come out from methanol rectification post (6), through pipeline (51), enter in the methanol vapor sparger (44) by methanol vapor inlet (53), and methanol vapor is entered into reactor (23) equably by the check valve on the methanol vapor sparger (54), carry out esterification with lipid acid, the water that produces arrives condenser (11) by pipeline (12) together with vapor form and unreacted methanol steam, and condensed aqueous methanol turns back to methanol gasifying reactor (1).Realized like this water that esterification produces is constantly removed, esterification is carried out continuously fast.When esterification reaches requirement (esterification yield reaches more than 99%), close well heater (2,43) and stir pump (49), regulate T-valve (8) the residue methanol vapor is recovered in the methanol gasifying reactor (1) by condenser (11).Material in esterification, the transesterification reactor (23) is placed for some time, and the catalyzer with lower floor after the layering is discharged in the glycerine storage tank (48) by T-valve (47).After feed separation finishes, close T-valve (47), regulate T-valve (46) and two-port valve (17 simultaneously, 18,20,45), open well heater (41,43), the temperature that temperature in the controlling reactor (23) remains in 180～250 ℃ and the steam generator (24) remains on 100 ± 5 ℃, make reactor (23), steam generator (24), material in water-and-oil separator (28) and the biofuel collector (31) forms following circulation: the water vapor that steam generator (24) produces is through pipeline (42), enter into esterification equably by methanol vapor sparger (44), in the transesterification reactor (23), and fatty acid methyl ester led out, arrive condenser (29) by pipeline (25), condensed water-oil mixture body enters water-and-oil separator (28) by condensate outlet (37), realize separating of oil and water, the water of lower floor turns back to steam generator (24) through pipeline (39).Circulation by water vapor, highly purified fatty acid methyl ester constantly is brought to water-and-oil separator (28), and enter biofuel collector (31) by pipeline (32), carry out further oily water separation at this, final highly purified fatty acid methyl ester is that biofuel is passed through valve (33) and constantly collected in the product storage tank (34).
The raw material input amount of present embodiment is a double centner, and an acidic catalyst sulfuric acid input amount is 1 kilogram, and reaction time of esterification is 110 minutes, and esterification yield reaches 99.54%.Thick product is refining through steam distillation, and yield is 99.86%, and product purity is 99.96%.
Embodiment 2: the catering trade waste oil is the feedstock production biofuel
Catering trade waste oil (acid number is 163.0) is a high-acid-value material, and the operating process that high-acid-value material prepares biofuel is: the esterification acid reduction process is identical with the esterification acid reduction process of embodiment 1.When acid number less than 5.0 the time, close well heater (2,43) and stir pump (49), regulate T-valve (8) the residue methanol vapor be recovered in the methanol gasifying reactor (1) by condenser (11).Material standing demix in the reactor (23), catalyzer and a spot of glycerine with lower floor after the layering are discharged in the glycerine storage tank (48) by T-valve (47).After feed separation finishes, close T-valve (47), regulating T-valve (4,46,50) simultaneously quantitatively is added to the methyl alcohol in the methyl alcohol storage tank (5) in the reactor (23) by pipeline (3), and regulate two-port valve (17,18,20,45), make esterification, transesterification reactor (23) become a reflux.Start and stir pump (49), under constantly stirring, by two-port valve (13) the basic catalyst methanol solution in the basic catalyst storage tank (14) is joined in the reactor (23), start well heater (43), material temperature is between 60～70 ℃ in the controlling reactor (23), the methanol vapor that produces is got back in the reactor (23) through reflux condensation mode post (19) condensation, and raw material carries out transesterification reaction continuously at reactor (23).Stop heating when conversion of raw material reaches requirement (getting final product more than 90%), stir, standing demix is discharged into lower floor's (glycerin layer) in the glycerine storage tank (48) by T-valve (47), is used to reclaim glycerine.The treating process of the thick product biofuel of upper strata (methyl esters layer) material is identical with the process of embodiment 1.
The raw material input amount of present embodiment is a double centner, and an acidic catalyst sulfuric acid input amount is 0.5%, and basic catalyst potassium hydroxide input amount is 0.4 kilogram.The esterification acid reduction time is 120 minutes, and acid number drops to 1.8 from 163.0, and the transesterification reaction time is 90 minutes, and transformation efficiency is 94.06%, and thick product is refining through steam distillation, and yield is 93.57%, and product purity is 99.38%.
Embodiment 3: rapeseed oil is the feedstock production biofuel
Rapeseed oil is an indeterminate plant oil, the operating process that with the neutral grease is the feedstock production biofuel is: neutral grease can directly be carried out transesterification reaction, the transesterify process is identical with the transesterify operating process of implementing 2, and is identical with the treating process of enforcement 1 and enforcement 2 to the treating process of thick product.
The raw material input amount of present embodiment is a double centner, and the basic catalyst input amount is 1 kilogram.The transesterification reaction time is 120 minutes, and transformation efficiency is 94.89%, and thick product is refining through steam distillation, and yield is 94.27%, and product purity is 99.04%.
Implement 4: be used for methanol rectification
The operating process of methanol rectification is: when being the raw material production biofuel with lipid acid and high-acid value grease, the water that produces in the esterification process is brought in the methanol gasifying device (1), when wherein water runs up to a certain degree, need carry out the separation of first alcohol and water, reclaim methyl alcohol.Specific operation process is: regulate T-valve (7,8) reactor (1) is become a methanol rectifying system.Start well heater (2), through the effect of methanol rectification post (6), methanol vapor is recovered in the methyl alcohol storage tank (5) after by condenser (11) condensation, has realized the refining of methyl alcohol, and the refining methanol remainder water is discharged by outlet (52).
Claims (1)
1, a kind of device for preparing biofuel, it is characterized in that this device is by methanol gasifying device (1), by pipeline (51) and T-valve (8), (50), (46) esterification that is connected with methanol gasifying device (1), transesterification reactor (23), by pipeline (42) and two-port valve (45) and esterification, the steam generator (24) that transesterification reactor (23) connects, by air pressure balance passage (27), the water-and-oil separator (28) that pipeline (39) and two-port valve (38) are connected with steam generator (24), by air pressure balance passage (30), the biofuel collector (31) of two-port valve (36) is equipped with in its underpart that biofuel discharge outlet (32) is connected with water-and-oil separator (28), forms by the product biofuel storage tank (34) that pipeline (35) and two-port valve (33) are connected with biofuel collector (31); Wherein:
A. the inside of methanol gasifying device (1) is provided with that the left side that well heater (2), top be provided with methanol rectification post (6), methanol gasifying device (1) is provided with the condenser (11) by T-valve (8) and pipe connection, methyl alcohol storage tank (5), the lower part outlet place that is connected with (4) and pipeline (3) by T-valve (7) is provided with connecting tube and two-port valve (52);
B. esterification, the inside of transesterification reactor (23) is provided with well heater (43), be connected and be equipped with on it methanol vapor sparger (44) of check valve (54) with methanol vapor inlet (53), be equipped with the retaining that stirs pump liquid influx (22) on it and pull (21), the top is provided with two-port valve (17), (18), (20) and pipeline (12), (25) condenser of Lian Jieing (19), the left side at top is provided with two-port valve (9) respectively, (13), (15) and the raw oil material storage tank (10) of pipe connection, basic catalyst storage tank (14), an acidic catalyst storage tank (16), esterification, the left side of transesterification reactor (23) is provided with the stirring pump (49) with pipe connection, the by product raw glycerine storage tank (48) that is connected with pipeline and T-valve (47);
C. the inside of steam generator (24) is provided with that well heater (41), top are provided with two-port valve (26), the lower part outlet place is provided with two-port valve (40);
D. the inside of water-and-oil separator (28) is provided with by pipeline and condenser (29) banded condensate outlet (37), condenser (29) that the top is provided with to be connected with pipeline (25).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2006200193433U CN200951999Y (en) | 2006-03-10 | 2006-03-10 | Apparatus for producing biological diesel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2006200193433U CN200951999Y (en) | 2006-03-10 | 2006-03-10 | Apparatus for producing biological diesel oil |
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| Publication Number | Publication Date |
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| CN200951999Y true CN200951999Y (en) | 2007-09-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2006200193433U Expired - Fee Related CN200951999Y (en) | 2006-03-10 | 2006-03-10 | Apparatus for producing biological diesel oil |
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| CN (1) | CN200951999Y (en) |
Cited By (8)
| 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 |
| CN101805673A (en) * | 2010-04-01 | 2010-08-18 | 江苏大学 | Airlifting biodiesel ester exchange reactor |
| CN101962599A (en) * | 2010-05-28 | 2011-02-02 | 王金华 | Complete equipment for refining commercial grease by utilizing illegal cooking oil and method thereof |
| CN103060097A (en) * | 2012-12-30 | 2013-04-24 | 上海油好同盟新能源科技有限公司 | Continuous production line for producing biodiesel under catalysis of solid catalyst |
| CN103436282A (en) * | 2013-09-04 | 2013-12-11 | 常影 | Method and equipment for producing liquid fuel oil by catalytically modifying methanol fuel and waste oil |
| CN105112168A (en) * | 2015-08-21 | 2015-12-02 | 中国石油大学(华东) | Biodiesel producing device and method |
| CN105602738A (en) * | 2014-12-30 | 2016-05-25 | 浙江大学 | Device for preparing biodiesel from microalgae biomass by means of ester exchange and then extraction |
| CN105969530A (en) * | 2016-05-18 | 2016-09-28 | 淮南泉润环保科技有限公司 | Method for continuously producing biodiesel from scrapped animal and vegetable oil |
-
2006
- 2006-03-10 CN CNU2006200193433U patent/CN200951999Y/en not_active Expired - Fee Related
Cited By (11)
| 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 |
| CN101805673A (en) * | 2010-04-01 | 2010-08-18 | 江苏大学 | Airlifting biodiesel ester exchange reactor |
| CN101962599A (en) * | 2010-05-28 | 2011-02-02 | 王金华 | Complete equipment for refining commercial grease by utilizing illegal cooking oil and method thereof |
| CN103060097A (en) * | 2012-12-30 | 2013-04-24 | 上海油好同盟新能源科技有限公司 | Continuous production line for producing biodiesel under catalysis of solid catalyst |
| CN103060097B (en) * | 2012-12-30 | 2014-11-26 | 上海油好同盟新能源科技有限公司 | Continuous production line for producing biodiesel under catalysis of solid catalyst |
| CN103436282A (en) * | 2013-09-04 | 2013-12-11 | 常影 | Method and equipment for producing liquid fuel oil by catalytically modifying methanol fuel and waste oil |
| CN103436282B (en) * | 2013-09-04 | 2015-07-08 | 常影 | Method and equipment for producing liquid fuel oil by catalytically modifying methanol fuel and waste oil |
| CN105602738A (en) * | 2014-12-30 | 2016-05-25 | 浙江大学 | Device for preparing biodiesel from microalgae biomass by means of ester exchange and then extraction |
| CN105112168A (en) * | 2015-08-21 | 2015-12-02 | 中国石油大学(华东) | Biodiesel producing device and method |
| CN105112168B (en) * | 2015-08-21 | 2018-10-26 | 中国石油大学(华东) | A kind of device and method producing biodiesel |
| CN105969530A (en) * | 2016-05-18 | 2016-09-28 | 淮南泉润环保科技有限公司 | Method for continuously producing biodiesel from scrapped animal and vegetable oil |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20070926 Termination date: 20100310 |