CN104087412A - Process and equipment for fatty acid methyl ester refining - Google Patents
Process and equipment for fatty acid methyl ester refining Download PDFInfo
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- CN104087412A CN104087412A CN201410348781.3A CN201410348781A CN104087412A CN 104087412 A CN104087412 A CN 104087412A CN 201410348781 A CN201410348781 A CN 201410348781A CN 104087412 A CN104087412 A CN 104087412A
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- pipeline
- tank
- canned
- methyl ester
- well heater
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The invention provides a process and equipment for fatty acid methyl ester fining, and the process and the equipment are used for obtaining biodiesel with high purity and high yield; as shown in figure, 1 represents a shield pump, 2 represents a heater, 3 represents a heat exchanger, 4 represents a heater, 5 represents a glycerol separating tank, 6 represents a collecting tank, 7 represents a shield pump, 8 represents a flow rate meter, 9 represents a heater, 10 represents a methyl ester distillation tower, 11 represents a finished product cooler, 12 represents a finished product receiving tank, 13 represents a shield pump, 14 represents a re-boiler, 15 represents a shield pump, 16 represents a pre-heater, 17represents a cooler, 18 represents a cold trap, 19 represents a buffer tank, 20 represents a filler box, 21 represents a collecting tank, 22 represents a shield pump, 23 represents a vacuum machine set, 24 represents a vacuum cooler, and 25 represents a vacuum pump cooling water tank.
Description
Technical field
The present invention relates to the refining Processes and apparatus of a kind of fatty acid methyl ester, belong to chemical field, relate to particularly a kind of with the refining Processes and apparatus of the product fatty acid methyl ester of waste oil esterification process production biofuel to obtain the biofuel of high yield high-quality.
Background technology
What waste oil referred to that food production or marketing unit produces in business process can not be edible again animal-plant oil, comprise after grease uses, produce can not be edible again grease, what catering trade waste grease and oil-containing waste water produced after water-and-oil separator or oil trap separate can not be edible again grease.For example: the waste oil that non-edible lard, hogwash fat, the lampblack absorber that frying waste oil, the industrial pigskin chopped cooked entrails of sheep boil discharges etc.The output of China's waste oil is very large, it is estimated, the amount of waste grease accounts for the 20%-30% of edible oil aggregate consumption.Consume every year edible oil 21Mt in China, produce every year waste oil 4-8Mt.Collect and can have 4Mt left and right as the waste grease of the utilization of resources.It is reported, restaurant, incity, Beijing just can produce about 20t waste oil for one day, more than can reaching 7kt every year.China is again liquefaction big country in the world, every year can be more than processing and eating oil 10Mt, and have the bone product processing enterprises such as several thousand edible oils and meat, leather, bone meal, gelatine, gelatin, can discharge every year the millions of tons of animal-plant oil tankage.If these waste oils and animal and vegetable oil leftover directly discharge, not only cause environment and water pollution, and be a kind of serious wasting of resources.It is reported, the about 2Mt edible oil of the annual use of Japan, produces 400-600kt waste edible oil, wherein has 250-260kt to be recycled.At present, the major industry purposes of utilizing food and beverage waste oil and grease and animal and vegetable oil leftover is to produce the Chemicals such as oil, soap, coating and washing composition animal-feed for, has serious potential safety hazard with the animal-feed of waste edible oil fat interpolation, is forbidded strictly.In order thoroughly to stop the harm of waste edible oil fat and animal and vegetable oil leftover, improve its utility value, finding the new approach that utilizes has become the task of top priority, and using it for production biofuel is a good developing direction.
Because waste oil is mostly corrupt serious, acid number is very high, main component is glycerin fatty acid ester and lipid acid, and wherein lipid acid and methyl alcohol carry out esterification generation fatty acid methyl ester and water, and glycerin fatty acid ester and methyl alcohol carry out transesterification reaction and generates fatty acid methyl ester and glycerine.Simultaneously because the catalyzer of reaction is strong acid and strong base, there is complicated oxidation and polyreaction generates biological pitch in organism under the effect of strong acid and strong base, the existence of biological pitch and glycerine seriously affects the quality of biofuel, must be isolated so that fatty acid methyl ester is refined.
Summary of the invention
In order to overcome the above problems, the invention provides a kind of fatty acid methyl ester refining Processes and apparatus, to obtain the biofuel of high yield high-quality.
To achieve these goals, the technical scheme of the refining process using of the invention fatty acid methyl ester is:
(1) after under meter metering, squeeze into well heater 2 by canned-motor pump 1 from the raw material esterification reaction product in esterification workshop, well heater 2 is by heat-conducting oil heating, and the temperature of thermal oil is controlled at 200 to 280 DEG C, and material is heated to 80 to 120 DEG C at this;
(2) material enters tower top interchanger 3 and is further warmed up to 100 to 140 DEG C with overhead vapours heat exchange after being heated;
(3) material after heat exchange enters well heater 4 and is further warmed up to 120 to 160 DEG C, then enter glycerine separating tank 5, glycerin vapor enters holding tank 21 by the Base top contact of glycerine separating tank after water cooler 17 is cooling, squeeze into glycerine storage tank finally by canned-motor pump 22, water cooler 17 and holding tank 21 are all connected with vacuum unit 23 through cold-trap 18, surge tank 19 and stuffing box 20, and vacuum unit is connected with vacuum pump water cooler 24 and vacuum pump water tank 25 again;
(4) material removing after glycerine enters holding tank 6, then squeezes into methyl ester distilled tower 10 by canned-motor pump 7 through under meter 8, well heater 9;
(5) pitch is discharged and is squeezed into asphalt tank by canned-motor pump 15 by reboiler 14 bottom, if in pitch when the too high levels of fatty acid methyl ester, further separates by squeezing into methyl ester distilled tower 10 after canned-motor pump 15 heater via 16 preheatings;
(6) fatty acid methyl ester is drawn and after finished product water cooler 11 is cooling, is entered finished product receiving tank 12 by the top of methyl ester distilled tower 10, then it is for sale to squeeze into finished product fatty acid methyl ester oil tank by canned-motor pump 13.
The beneficial effect of the invention is:
1, adopt folder point analysis method design production technique, utilized to greatest extent the various waste heats in producing, reach energy-saving and cost-reducing object;
2, through a large amount of production practice, optimize manufacturing condition, shortened the production cycle, improved labour productivity.
Brief description of the drawings
Accompanying drawing is the process flow diagram of the invention, wherein 1 is canned-motor pump, the 2nd, well heater, the 3rd, interchanger, the 4th, well heater, the 5th, glycerine separating tank, the 6th, holding tank, the 7th, canned-motor pump, the 8th, under meter, the 9th, well heater, the 10th, methyl ester distilled tower, the 11st, finished product water cooler, the 12nd, finished product receiving tank, the 13rd, canned-motor pump, the 14th, reboiler, the 15th, canned-motor pump, the 16th, preheater, the 17th, water cooler, the 18th, cold-trap, the 19th, surge tank, the 20th, stuffing box, the 21st, holding tank, the 22nd, canned-motor pump, the 23rd, vacuum unit, the 24th, vacuum pump water cooler, the 25th, vacuum pump cooling water tank.
As shown in drawings, the equipment of the refining technique of a kind of fatty acid methyl ester: by canned-motor pump (1), well heater (2), interchanger (3), well heater (4), glycerine separating tank (5), holding tank (6), canned-motor pump (7), under meter (8), well heater (9), methyl ester distilled tower (10), finished product water cooler (11), finished product receiving tank (12), canned-motor pump (13), reboiler (14), canned-motor pump (15), preheater (16), water cooler (17), cold-trap (18), surge tank (19), stuffing box (20), holding tank (21), canned-motor pump (22), vacuum unit (23), vacuum pump water cooler (24), the compositions such as vacuum pump cooling water tank (25), wherein well heater (2), well heater (4), well heater (9), reboiler (14), preheater (16) etc. all adopts heat-conducting oil heating, wherein canned-motor pump (1) is connected with well heater (2) by pipeline, well heater (2) is connected with interchanger (3) by pipeline, interchanger (3) is connected with well heater (4) by pipeline, well heater (4) is connected with glycerine separating tank (5) by pipeline, glycerine separating tank (5) is connected with holding tank (6) by pipeline, holding tank (6) is connected with canned-motor pump (7) by pipeline, canned-motor pump (7) is connected with under meter (8) by pipeline, under meter (8) is connected with well heater (9) by pipeline, well heater (9) is connected with methyl ester distilled tower (10) by pipeline, methyl ester distilled tower (10) is by pipeline and finished product water cooler (11), reboiler (14) and preheater (16) are connected, finished product water cooler (11) is connected with finished product receiving tank (12) by pipeline, finished product receiving tank (12) is connected with canned-motor pump (13) by pipeline, reboiler (14) is connected with canned-motor pump (15) by pipeline, canned-motor pump (15) is connected with preheater (16) by pipeline, preheater (16) is connected with methyl ester distilled tower (10) by pipeline, methyl ester distilled tower (10) top is connected with water cooler (17) by pipeline, water cooler (17) is connected with cold-trap (18) by pipeline, cold-trap (18) is connected with surge tank (19) by pipeline, surge tank (19) is connected with stuffing box (20) by pipeline, stuffing box (20) is connected with holding tank (21) and vacuum unit (23) by pipeline, holding tank (21) is connected with canned-motor pump (22) by pipeline, vacuum unit (23) is connected with vacuum pump water cooler (24) and vacuum pump cooling water tank (25) respectively by pipeline, vacuum pump water cooler (24) is connected with vacuum pump cooling water tank (25) by pipeline, vacuum pump cooling water tank (25) is connected with vacuum unit (23) and vacuum pump water cooler (24) by pipeline.
Claims (2)
1. the refining technique of fatty acid methyl ester, it is characterized in that: (1) squeezes into well heater 2 by canned-motor pump 1 from the raw material esterification reaction product in esterification workshop after under meter metering, well heater 2 is by heat-conducting oil heating, the temperature of thermal oil is controlled at 200 to 280 DEG C, and material is heated to 80 to 120 DEG C at this;
(2) material enters tower top interchanger 3 and is further warmed up to 100 to 140 DEG C with overhead vapours heat exchange after being heated;
(3) material after heat exchange enters well heater 4 and is further warmed up to 120 to 160 DEG C, then enter glycerine separating tank 5, glycerin vapor enters holding tank 21 by the Base top contact of glycerine separating tank after water cooler 17 is cooling, squeeze into glycerine storage tank finally by canned-motor pump 22, water cooler 17 and holding tank 21 are all connected with vacuum unit 23 through cold-trap 18, surge tank 19 and stuffing box 20, and vacuum unit is connected with vacuum pump water cooler 24 and vacuum pump water tank 25 again;
(4) material removing after glycerine enters holding tank 6, then squeezes into methyl ester distilled tower 10 by canned-motor pump 7 through under meter 8, well heater 9;
(5) pitch is discharged and is squeezed into asphalt tank by canned-motor pump 15 by reboiler 14 bottom, if in pitch when the too high levels of fatty acid methyl ester, further separates by squeezing into methyl ester distilled tower 10 after canned-motor pump 15 heater via 16 preheatings;
(6) fatty acid methyl ester is drawn and after finished product water cooler 11 is cooling, is entered finished product receiving tank 12 by the top of methyl ester distilled tower 10, then it is for sale to squeeze into finished product fatty acid methyl ester oil tank by canned-motor pump 13.
2. the equipment of the refining technique of fatty acid methyl ester according to claim 1, it is characterized in that: by canned-motor pump (1), well heater (2), interchanger (3), well heater (4), glycerine separating tank (5), holding tank (6), canned-motor pump (7), under meter (8), well heater (9), methyl ester distilled tower (10), finished product water cooler (11), finished product receiving tank (12), canned-motor pump (13), reboiler (14), canned-motor pump (15), preheater (16), water cooler (17), cold-trap (18), surge tank (19), stuffing box (20), holding tank (21), canned-motor pump (22), vacuum unit (23), vacuum pump water cooler (24), the compositions such as vacuum pump cooling water tank (25), wherein well heater (2), well heater (4), well heater (9), reboiler (14), preheater (16) etc. all adopts heat-conducting oil heating, wherein canned-motor pump (1) is connected with well heater (2) by pipeline, well heater (2) is connected with interchanger (3) by pipeline, interchanger (3) is connected with well heater (4) by pipeline, well heater (4) is connected with glycerine separating tank (5) by pipeline, glycerine separating tank (5) is connected with holding tank (6) by pipeline, holding tank (6) is connected with canned-motor pump (7) by pipeline, canned-motor pump (7) is connected with under meter (8) by pipeline, under meter (8) is connected with well heater (9) by pipeline, well heater (9) is connected with methyl ester distilled tower (10) by pipeline, methyl ester distilled tower (10) is by pipeline and finished product water cooler (11), reboiler (14) and preheater (16) are connected, finished product water cooler (11) is connected with finished product receiving tank (12) by pipeline, finished product receiving tank (12) is connected with canned-motor pump (13) by pipeline, reboiler (14) is connected with canned-motor pump (15) by pipeline, canned-motor pump (15) is connected with preheater (16) by pipeline, preheater (16) is connected with methyl ester distilled tower (10) by pipeline, methyl ester distilled tower (10) top is connected with water cooler (17) by pipeline, water cooler (17) is connected with cold-trap (18) by pipeline, cold-trap (18) is connected with surge tank (19) by pipeline, surge tank (19) is connected with stuffing box (20) by pipeline, stuffing box (20) is connected with holding tank (21) and vacuum unit (23) by pipeline, holding tank (21) is connected with canned-motor pump (22) by pipeline, vacuum unit (23) is connected with vacuum pump water cooler (24) and vacuum pump cooling water tank (25) respectively by pipeline, vacuum pump water cooler (24) is connected with vacuum pump cooling water tank (25) by pipeline, vacuum pump cooling water tank (25) is connected with vacuum unit (23) and vacuum pump water cooler (24) by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410348781.3A CN104087412A (en) | 2014-07-17 | 2014-07-17 | Process and equipment for fatty acid methyl ester refining |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410348781.3A CN104087412A (en) | 2014-07-17 | 2014-07-17 | Process and equipment for fatty acid methyl ester refining |
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| Publication Number | Publication Date |
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| CN104087412A true CN104087412A (en) | 2014-10-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201410348781.3A Pending CN104087412A (en) | 2014-07-17 | 2014-07-17 | Process and equipment for fatty acid methyl ester refining |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106929162A (en) * | 2017-03-30 | 2017-07-07 | 迈安德集团有限公司 | A kind of utilization waste grease produces the deacidification technique of glycerine |
| CN115386432A (en) * | 2022-07-29 | 2022-11-25 | 湖南诺睿信生物科技有限公司 | System for producing biodiesel by using double enzymes and production method thereof |
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| CN101020838A (en) * | 2007-03-23 | 2007-08-22 | 江西新时代油脂工业有限公司 | Biodiesel oil preparing process and apparatus |
| CN201125232Y (en) * | 2007-11-14 | 2008-10-01 | 山东省花生研究所 | Biological diesel oil distilling tower |
| CN202912929U (en) * | 2013-02-18 | 2013-05-01 | 广西合众能源股份有限公司 | Continuous production equipment for biodiesel |
| US8491857B1 (en) * | 2012-03-09 | 2013-07-23 | Antonio Cantizani | Processes and apparatus for small-scale in situ biodiesel production |
-
2014
- 2014-07-17 CN CN201410348781.3A patent/CN104087412A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101020838A (en) * | 2007-03-23 | 2007-08-22 | 江西新时代油脂工业有限公司 | Biodiesel oil preparing process and apparatus |
| CN201125232Y (en) * | 2007-11-14 | 2008-10-01 | 山东省花生研究所 | Biological diesel oil distilling tower |
| US8491857B1 (en) * | 2012-03-09 | 2013-07-23 | Antonio Cantizani | Processes and apparatus for small-scale in situ biodiesel production |
| CN202912929U (en) * | 2013-02-18 | 2013-05-01 | 广西合众能源股份有限公司 | Continuous production equipment for biodiesel |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106929162A (en) * | 2017-03-30 | 2017-07-07 | 迈安德集团有限公司 | A kind of utilization waste grease produces the deacidification technique of glycerine |
| CN106929162B (en) * | 2017-03-30 | 2020-09-15 | 迈安德集团有限公司 | Acid reducing process for producing glycerol by using waste oil |
| CN115386432A (en) * | 2022-07-29 | 2022-11-25 | 湖南诺睿信生物科技有限公司 | System for producing biodiesel by using double enzymes and production method thereof |
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