CN102108319B - Continuous system and method for preparing biodiesel - Google Patents
Continuous system and method for preparing biodiesel Download PDFInfo
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- CN102108319B CN102108319B CN200910262781.0A CN200910262781A CN102108319B CN 102108319 B CN102108319 B CN 102108319B CN 200910262781 A CN200910262781 A CN 200910262781A CN 102108319 B CN102108319 B CN 102108319B
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02E50/10—Biofuels, e.g. bio-diesel
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Abstract
The invention discloses a continuous system and a continuous method for preparing biodiesel. The continuous method for preparing biodiesel comprises the following steps: (a) pressurizing and heating liquid alcohol till the liquid alcohol changes into a subcritical state or high-pressure liquid state; (b) performing continuous extraction by using a continuous extraction module which has a plurality of extraction tanks for receiving the subcritical or high-pressure liquid alcohol, extracting a grease raw material in the extraction tanks, and obtaining an extract product; (c) performing the transesterification of the extract product to obtain a product of the transesterification; and (d) separating the product of the transesterification to obtain the biodiesel. In the continuous system and the continuous method for preparing biodiesel, the biodiesel is prepared by extracting the grease with the subcritical or high-pressure liquid alcohol and the transesterification of supercritical alcohol, the continuous extraction module and the continuous extraction method are used for extraction, the extraction and transesterification process procedures are performed by using the same alcohol, the process is simplified, and labor force and energy are saved.
Description
Technical field
The present invention, relevant for a kind of system and method for preparing biofuel, in detail, is the continous way system and method for preparing biofuel about a kind of.
Background technology
Traditional biological diesel oil (biodiesel) is to complete with alkali technique or sour technique, but because needs are used soda acid catalyst or reactant, often causes the puzzlement of back segment purifying products and recycling.Current legal biofuel factory, all belong to first-generation technology and take U.S.'s rule as main, reaction time of esterification is long, transformation efficiency is not high, owing to using acid and alkali raw material, liquid waste disposal is a large problem, contain impurity (as saponified) more again, must rectifying just can reach industrial standards, cost is higher.
At present also have several technique of improving traditional biological diesel oil method, two-stage transesterification technology of preparing is wherein a kind of, but also has shortcomings; In addition, though biological transesterification has the advantages such as can directly transform free fatty acids and glycerine is easily separated, owing to using, biocatalyzer thereby cost are higher, and speed of reaction is slower; Still many at Literature Discussion at present as for solid-state catalyst method, not yet there is industrialization actual achievement.
United States Patent (USP) the 6th, 211,390 No. B1, patent name is " Method for producing fattyacid " (fatty acid ester manufacture method), disclosed a kind of method of utilizing supercritical extraction to prepare biofuel, this patent is to be rich in the raw material of triglyceride, under alkaline catalyst effect, carry out transesterification with alcohols, the fatty acid ester and the complete excessive alcohols reactant of unreacted that generate, via near or supercutical fluid, under out-phase catalysis, carry out extracting and separating again, obtain highly purified biofuel.This patent shortcoming is to limit to some extent manufacturing biodiesel raw material, cannot be widely used in the oil sources of moisture or free fatty acids; Moreover reactant methanol needs excessively in turning esterification process, with supercutical fluid, under out-phase catalysis, carry out methanol extraction separation, may need to consume the object that a large amount of energy can reach high separation and purification.
No. 466271 patent of TaiWan, China patent announcement, title " is manufactured the method for the alkyl ester of lipid acid " from lipid, disclosed a kind of do not need to use metal base catalyst or sour catalyst, and under overcritical lower alcohol state, the method for biofuel is prepared in transesterification.This patent is lipid raw material and the reaction of low-carbon (LC) alcohols that can use containing free fatty acids, and Witepsol W-S 55 contained in lipid is carried out under overcritical alcohols state to transesterification to manufacture the alkyl ester of lipid acid, simultaneously owing to reacting under the condition not using metal base catalyst, sour catalyst, can not need to carry out the pre-treatment step by Esterification of Free Fat Acid, and can not generate the by product of fatty acid soaps, thereby can omit or simplify the purification and recover step of resultant.This patent only limits to manufacture with supercritical methanol the method for the alkyl ester of lipid acid, and raw material may be waste edible oil or biomass grease.
In " Semen Brassicae campestris and supercritical methanol situ extracting-ester permutoid reaction are prepared biofuel " document of China's " applied chemistry periodical " the 23rd the 12nd phase of volume, point out: directly utilize Semen Brassicae campestris and supercritical methanol effect to prepare biofuel, supercritical extraction and overcritical transesterification reaction can be combined, utilize supercritical extraction to improve the percentage extraction of grease in vegetable seed on the one hand; Supercritical extraction and overcritical transesterification reaction are carried out in same reactor simultaneously on the other hand, can save the program of oil expression, the production cost of reduction biofuel.About the supercritical methanol technology extraction of Vegetable oil lipoprotein, studying at present more is supercritical CO
2extraction process, the document adopt Supercritical methanol carry out grease extraction and by supercritical extraction and overcritical transesterification reaction combine prepare biofuel research at present all without reported in literature.Yet best extraction is not identical with service temperature and the pressure condition of transesterification, and in same reactor, carry out supercritical extraction and overcritical transesterification turns to batch operation simultaneously, and cannot reach continuous process.
Therefore, be necessary to provide the continous way system and method for the preparation biofuel of a kind of innovation and tool progressive, to address the above problem.
Summary of the invention
For solving the problems of the technologies described above, the object of the present invention is to provide a kind of continous way system and method for preparing biofuel, by continous way, extract and overcritical alcohols transesterification, prepare biofuel, have the advantages that technique is simple, cost is low.
For achieving the above object, first the present invention provides a kind of continous way system of preparing biofuel, comprising:
One liquid alcohol storage tanks, in order to storing liquid alcohol;
One continous way extraction module, has most extraction tanks, and described extraction tank is in order to receive liquid alcohol, and the glyceride stock in extraction tank is extracted, and to obtain extraction product, and reaches continuous extraction;
One tubular type transesterification device, in order to receive extraction product, to carry out transesterification, obtains turning esterification products; And
One first gas-liquid separation groove, turns esterification products in order to separation, to obtain biofuel.
In above-mentioned continous way system, preferably, this continous way system also comprises one first liquid pump and one first preheater, in order to pressurize and to heat described liquid alcohol to subcritical state or high-pressure liquid.
In above-mentioned continous way system, preferably, described continous way extraction module comprises three extraction tanks, in order to carry out respectively the alternately operating of glyceride stock filling, extraction and blowdown.
In above-mentioned continous way system, preferably, described glyceride stock is the material plant that is rich in triglyceride, and extraction product is triglyceride and alcohol.
In above-mentioned continous way system, preferably, this continous way system also comprises one second preheater, in order to heat extraction product.More preferably, this continous way system also comprises a vacuum breaker, is arranged between described the second preheater and described continous way extraction module.
In above-mentioned continous way system, preferably, described tubular type transesterification device is maintained at above-critical state operational condition.
In above-mentioned continous way system, preferably, described the first gas-liquid separation groove is in order to be liquid phase by transesterification product separation fatty acid ester, glycerine, and the alcohols of gas phase.More preferably, this continous way system also comprises a condenser, is arranged between described the first gas-liquid separation groove and described liquid alcohol storage tanks, in order to the alcohols condensation of gas phase is imported to described liquid alcohol storage tanks.
In above-mentioned continous way system, preferably, this continous way system also comprises a CO
2storage tank, one first condenser, one second liquid pump and one second preheater, wherein this CO
2storage tank is in order to store CO
2, this first condenser is in order to by CO
2be condensed into liquid state, this second liquid pump is by liquid CO
2add this second preheater, this second preheater is in order to by liquid CO
2and extraction product heating.
In above-mentioned continous way system, preferably, described tubular type transesterification device is in order to receive extraction product and CO
2, to carry out transesterification, obtain turning esterification products; Described the first gas-liquid separation groove is in order to be liquid phase by transesterification product separation fatty acid ester, glycerine, and the alcohols of gas phase and CO
2.
In above-mentioned continous way system, preferably, this continous way system also comprises one second gas-liquid separation groove, in order to receive alcohols and the CO of gas phase
2, be separated into the alcohols of liquid phase and the CO of gas phase
2, the alcohols of liquid phase imports described liquid alcohol storage tanks.
In above-mentioned continous way system, preferably, this continous way system also comprises one second condenser, is arranged at described the second gas-liquid separation groove and described CO
2between storage tank, in order to by the CO of gas phase
2condensation imports described CO
2storage tank.
The present invention also provides a kind of continous way method of preparing biofuel, comprises the following steps:
(a) liquid towards alcohol pressurizes and is heated to subcritical state or high-pressure liquid;
(b) utilize a continous way extraction module to carry out continuous extraction, wherein this continous way extraction module has most extraction tanks, described extraction tank is in order to receive subcritical state or high-pressure liquid alcohol, and the glyceride stock in extraction tank is extracted, to obtain extraction product;
(c) extraction product is carried out to transesterification, to obtain turning esterification products; And
(d) separation turns esterification products, to obtain biofuel.
In above-mentioned continous way method, preferably, in step (b), described continous way extraction module comprises three extraction tanks, in order to carry out respectively the alternately operating of glyceride stock filling, extraction and blowdown.
In above-mentioned continous way method, preferably, in step (b), described glyceride stock is the material plant that is rich in triglyceride, and extraction product is triglyceride and alcohol.
In above-mentioned continous way method, preferably, after step (b), the method also comprises a heating steps, in order to heat extraction product.
In above-mentioned continous way method, preferably, in step (c), be maintained at above-critical state operational condition and carry out transesterification.
In above-mentioned continous way method, preferably, in step (d), the fatty acid ester that is liquid phase by transesterification product separation, glycerine, and the alcohols of gas phase.
In above-mentioned continous way method, preferably, after step (d), the method also comprises a condensing steps, in order to by the alcohols condensation of gas phase.
In above-mentioned continous way method, preferably, front in step (c), the method also comprises that one provides CO
2step, it comprises condensation CO
2for liquid step, liquid CO pressurizes
2step and heat liquid CO
2and the step of extraction product.
In above-mentioned continous way method, preferably, in step (c), transesterification extraction product and CO
2, to obtain turning esterification products.
In above-mentioned continous way method, preferably, in step (d), comprise one first gas-liquid separation step, in order to separation, turn fatty acid ester, the glycerine that esterification products is liquid phase, and the alcohols of gas phase and CO
2.
In above-mentioned continous way method, preferably, in step (d), the method also comprises one second gas-liquid separation step, in order to receive alcohols and the CO of gas phase
2, be separated into the alcohols of liquid phase and the CO of gas phase
2.
In above-mentioned continous way method, preferably, after the second gas-liquid separation step, separately comprise a condensing steps, in order to by the CO of gas phase
2condensation.
The invention provides a kind of continous way system of preparing biofuel, comprising: a liquid alcohol storage tanks, continous way extraction module, a tubular type transesterification device and an one first gas-liquid separation groove.This liquid alcohol storage tanks is in order to storing liquid alcohol.This continous way extraction module has most extraction tanks, and at least one of them extraction tank is in order to receive liquid alcohol, and the glyceride stock in extraction tank is extracted, and to obtain extraction product, and reaches continuous extraction.This tubular type transesterification device, in order to receive extraction product, to carry out transesterification, obtains turning esterification products.This first gas-liquid separation groove turns esterification products in order to separation, to obtain biofuel.
The present invention separately provides a kind of continous way method of preparing biofuel, comprises the following steps: (a) pressurization and heating liquid alcohol are to subcritical state or high-pressure liquid; (b) utilize a continous way extraction module to carry out continuous extraction, wherein this continous way extraction module has most extraction tanks, described extraction tank is in order to receive subcritical state or high-pressure liquid alcohol, and the glyceride stock in extraction tank is extracted, to obtain extraction product; (c) extraction product is carried out to transesterification, to obtain turning esterification products; And (d) separation turns esterification products, to obtain biofuel.
The continous way system and method that the present invention prepares biofuel utilizes subcritical state or high-pressure liquid alcohols oil and grease extracting and prepares biofuel with overcritical alcohols transesterification, and extract via continous way extraction module and method, carry out again overcritical alcohols transesterification, in system and method, adopt identical alcohols to extract simultaneously and turn esterification procedure, can simplify technique, save manpower and the energy.
Accompanying drawing explanation
Fig. 1 shows the schematic diagram of the continous way system of the preparation biofuel that the embodiment of the present invention 1 provides;
Fig. 2 shows the schematic diagram of the continous way system of the preparation biofuel that the embodiment of the present invention 2 provides.
Primary clustering nomenclature:
The continous way system 10 of the embodiment of the present invention 1 preparation biofuel; Liquid alcohol storage tanks 11;
The first liquid pump, 12; The first preheater, 13; Continous way extraction module, 14; Vacuum breaker 15;
The second preheater, 16; Tubular type transesterification device, 17; The first gas-liquid separation groove, 18;
Condenser, 19; The continous way system, 30 of the embodiment of the present invention 2 preparation biofuel;
Liquid alcohol storage tanks, 31; The first liquid pump, 32; The first preheater, 33;
Continous way extraction module, 34; Vacuum breaker, 35; CO
2storage tank, 36; The first condenser, 37;
The second liquid pump, 38; The second preheater, 39; Tubular type transesterification device, 40;
The first gas-liquid separation groove, 41; The second gas-liquid separation groove, 42; The second condenser, 43;
The first extraction tank, 141; The second extraction tank, 142; The 3rd extraction tank, 143;
The first extraction tank, 341; The second extraction tank, 342; The 3rd extraction tank, 343.
Embodiment
Embodiment 1
With reference to figure 1, it shows the schematic diagram of the continous way system of the preparation biofuel that the embodiment of the present invention 1 provides.Below utilize Fig. 1 that the continous way system and method for the preparation biofuel that the embodiment of the present invention 1 provides is described.The continous way system 10 of the preparation biofuel that the embodiment of the present invention 1 provides comprises: a liquid alcohol storage tanks 11, continous way extraction module 14, a tubular type transesterification device 17 and an one first gas-liquid separation groove 18.This liquid alcohol storage tanks 11 is in order to storing liquid alcohol.
In the present embodiment, the continous way system 10 of preparation biofuel of the present invention separately comprises one first liquid pump 12 and one first preheater 13, in order to liquid alcohol is pressurizeed and be heated to subcritical state or high-pressure liquid.Wherein, subcritical state refers to that temperature maintains lower than 240 ℃ of critical temperatures and pressure higher than emergent pressure 80atm; High-pressure liquid refers to that temperature maintains lower than 240 ℃ of critical temperatures and pressure lower than emergent pressure 80atm.In addition, in the present embodiment, liquid alcohol can be the low-carbon alcohol of 1-5 carbon.
The liquid alcohol of subcritical state or high-pressure liquid imports this continous way extraction module 14.This continous way extraction module 14 has most extraction tanks 141,142,143, and wherein at least one extraction tank is in order to receive liquid alcohol, and the glyceride stock in extraction tank is extracted, and to obtain extraction product, and reaches continuous extraction.In the present embodiment, this continous way extraction module 14 comprises three extraction tanks 141,142,143, in order to carry out respectively the alternately operating of glyceride stock filling, extraction and blowdown.Preferably, these extraction tanks are high pressure extraction groove.
Illustrate, if when the first extraction tank 141 carries out glyceride stock filling, the second extraction tank 142 can extract, now, the liquid alcohol of subcritical state or high-pressure liquid imports the second extraction tank 142 and extracts, and the 3rd extraction tank 143 can carry out blowdown operation.After the second extraction tank 142 extractions, because the first extraction tank 141 glyceride stocks have loaded, the liquid alcohol of subcritical state or high-pressure liquid can be imported to the first extraction tank 141 and extract, the 3rd extraction tank 143 can carry out glyceride stock filling operation.Therefore, three extraction tanks 141,142,143, can carry out respectively the alternately operating of glyceride stock filling, extraction and blowdown, make to extract operation uninterrupted continuously.
In the present embodiment, this glyceride stock is the material plant that is rich in triglyceride, for example crush the crazy seed particle to 1-5mm granular size Ma, this liquid alcohol is selected methyl alcohol, because subcritical state methyl alcohol has splendid diffusion, matter passes and dissolving triglyceride ability, the sustainable about 0.5-2hr of extraction time.Therefore carry out oil extraction with subcritical state/high-pressure liquid alcohol, have that productive rate is high, the time is short, the optimum extraction conditions such as pressure and temperature are easy to the advantage of controlling.If oil plant raw material rich cellulose, in high pressure, be heated lower than 150 ℃, does not change to Mierocrystalline cellulose; High pressure, be heated higher than the coking of can dewatering of 150 ℃ of Mierocrystalline celluloses, but there is no impact for the extraction of triglyceride with the transesterification that continues.Therefore, the spendable raw material of continous way system 10 of preparation biofuel provided by the invention is wide, can contain large quantity of moisture, triglyceride and free fatty acids, and raw material does not need complete drying to process.
In the present embodiment, the extraction product through extraction tank is triglyceride and alcohol.The continous way system 10 of preparation biofuel provided by the invention separately comprises a vacuum breaker 15 and one second preheater 16.This vacuum breaker 15 is arranged between this second preheater 16 and this continous way extraction module 14.The second preheater 16, in order to heat extraction product, makes extraction product temperature higher than methanol critical temperature.
This tubular type transesterification device 17, in order to receive extraction product, to carry out transesterification, obtains turning esterification products.In the present embodiment, this tubular type transesterification device 17 is to be maintained at above-critical state operational condition, carries out supercritical methanol transesterification, and the suitableeest enzymatic synthesis condition that turns can be: it is 240 ℃-320 ℃ that service temperature is controlled, working pressure is controlled is 100-250atm.Turning esterification products comprises: fatty acid ester (biofuel), glycerine (byproduct) and the aqueous solution and unreacted methanol.The continous way system 10 of preparation biofuel provided by the invention is carried out transesterification with supercritical alcohols and is prepared biofuel, and transformation efficiency is higher, the reaction times is short, do not use soda acid catalyst, without soda acid, process problem again.
This first gas-liquid separation groove 18 turns esterification products in order to separation, to obtain biofuel.These the first gas-liquid separation groove 18 separation turn the fatty acid ester that esterification products is liquid phase (biofuel), glycerine to bottom land, and the alcohols of gas phase to groove pushes up.The continous way system 10 of preparation biofuel provided by the invention separately comprises a condenser 19, is arranged between this first gas-liquid separation groove 18 and this liquid alcohol storage tanks 11, in order to the alcohols condensation of gas phase is imported to this liquid alcohol storage tanks 11, reclaims use.
The continous way system 10 of the preparation biofuel that the embodiment of the present invention 1 provides is utilized subcritical state or high-pressure liquid alcohols oil and grease extracting and is prepared biofuel with overcritical alcohols transesterification, and extract via continous way extraction module and method, carry out again overcritical alcohols transesterification, in system and method, adopt identical alcohols to extract simultaneously and turn esterification procedure, can simplify technique, save manpower and the energy.
Embodiment 2
With reference to figure 2, it shows the schematic diagram of the continous way system of the preparation biofuel that the embodiment of the present invention 2 provides.The continous way system 30 of the preparation biofuel that the embodiment of the present invention 2 provides comprises: a liquid alcohol storage tanks 31, one first liquid pump 32, one first preheater 33, a continous way extraction module 34, a vacuum breaker 35, a CO
2storage tank 36, one first condenser 37, one second liquid pump 38, one second preheater 39, a tubular type transesterification device 40, one first gas-liquid separation groove 41, one second gas-liquid separation groove 42 and one second condenser 43.
The continous way system 10 of the preparation biofuel that the liquid alcohol storage tanks 31 of the continous way system 30 of the preparation biofuel that the embodiment of the present invention 2 provides, the first liquid pump 32, the first preheater 33, continous way extraction module 34 and vacuum breaker 35 provide with the embodiment of the present invention 1 is identical, and continous way extraction module 34 has the first extraction tank 341, the second extraction tank 342 and the 3rd extraction tank 343, no longer narration.
In the present embodiment, extraction product imports before the second preheater 39, adds the addition of C O
2.This CO wherein
2 storage tank 36 is in order to store CO
2, this first condenser 37 is in order to by CO
2be condensed into liquid state, this second liquid pump 38 is by liquid CO
2add this second preheater 39, this second preheater 39 receives liquid CO
2and extraction product, in order to by liquid CO
2and extraction product heating.
This tubular type transesterification device 40 is in order to receive extraction product and CO
2, to carry out transesterification, obtain turning esterification products.In the present embodiment, this tubular type transesterification device 40 is also maintained at above-critical state operational condition, carries out supercritical methanol transesterification, but because adding CO
2can make temperature and the pressure decreased of transesterification, to save electric energy.And because adding CO
2, turn esterification products and comprise: fatty acid ester (biofuel), glycerine (byproduct) and the aqueous solution and unreacted methanol and CO
2.
This first gas-liquid separation groove 41 turns in order to separation fatty acid ester, the glycerine that esterification products is liquid phase, and the alcohols of gas phase and CO
2.This second gas-liquid separation groove 42, in order to receive alcohols and the CO of gas phase
2, be separated into the alcohols of liquid phase and the CO of gas phase
2, the alcohols of liquid phase imports this liquid alcohol storage tanks 31 and reclaims use.This second condenser 43 is arranged at this second gas-liquid separation groove 42 and this CO
2between storage tank 36, in order to by the CO of gas phase
2condensation imports this CO
2storage tank 36 reclaims and uses.
Therefore, the continous way system and method for preparation biofuel provided by the invention utilizes subcritical state or high-pressure liquid alcohols oil and grease extracting and prepares biofuel with overcritical alcohols transesterification, and extract via continous way extraction module and method, carry out again overcritical alcohols transesterification, in system and method, adopt identical alcohols to extract simultaneously and turn esterification procedure, can simplify technique, save manpower and the energy.
Above-described embodiment is only explanation principle of the present invention and effect thereof, and unrestricted the present invention.Therefore, practise in the personage of this technology and above-described embodiment is modified and change still not de-spirit of the present invention.Claim scope is listed as described later for interest field of the present invention.
Claims (24)
1. a continous way system of preparing biofuel, comprising:
One liquid alcohol storage tanks, in order to storing liquid alcohol;
One continous way extraction module, has most extraction tanks, and described extraction tank is in order to receive liquid alcohol, and the glyceride stock in extraction tank is extracted, and to obtain extraction product, and reaches continuous extraction;
One tubular type transesterification device, in order to receive extraction product, to carry out transesterification, obtains turning esterification products; And
One first gas-liquid separation groove, turns esterification products in order to separation, to obtain biofuel;
This continous way system also comprises one first liquid pump and one first preheater, in order to pressurize and to heat described liquid alcohol to subcritical state or high-pressure liquid; Subcritical state refers to that temperature maintains lower than 240 ℃ of critical temperatures and pressure higher than emergent pressure 80atm; High-pressure liquid refers to that temperature maintains lower than 240 ℃ of critical temperatures and pressure lower than emergent pressure 80atm;
This continous way system also comprises one second preheater, in order to heat extraction product.
2. continous way system as claimed in claim 1, wherein, described continous way extraction module comprises three extraction tanks, in order to carry out respectively the alternately operating of glyceride stock filling, extraction and blowdown.
3. continous way system as claimed in claim 2, wherein, described glyceride stock is the material plant that is rich in triglyceride, extraction product is triglyceride and alcohol.
4. continous way system as claimed in claim 1, wherein, this continous way system also comprises a vacuum breaker, is arranged between described the second preheater and described continous way extraction module.
5. continous way system as claimed in claim 1, wherein, described tubular type transesterification device is maintained at above-critical state operational condition.
6. continous way system as claimed in claim 1, wherein, described the first gas-liquid separation groove is in order to be liquid phase by transesterification product separation fatty acid ester, glycerine, and the alcohols of gas phase.
7. continous way system as claimed in claim 6, wherein, this continous way system also comprises a condenser, is arranged between described the first gas-liquid separation groove and described liquid alcohol storage tanks, in order to the alcohols condensation of gas phase is imported to described liquid alcohol storage tanks.
8. continous way system as claimed in claim 1, wherein, this continous way system also comprises a CO
2storage tank, one first condenser, one second liquid pump and one second preheater, wherein this CO
2storage tank is in order to store CO
2, this first condenser is in order to by CO
2be condensed into liquid state, this second liquid pump is by liquid CO
2add this second preheater, this second preheater is in order to by liquid CO
2and extraction product heating.
9. continous way system as claimed in claim 8, wherein, described tubular type transesterification device is in order to receive extraction product and CO
2, to carry out transesterification, obtain turning esterification products.
10. continous way system as claimed in claim 9, wherein, described the first gas-liquid separation groove is in order to be liquid phase by transesterification product separation fatty acid ester, glycerine, and the alcohols of gas phase and CO
2.
11. continous way systems as claimed in claim 10, wherein, this continous way system also comprises one second gas-liquid separation groove, in order to receive alcohols and the CO of gas phase
2, be separated into the alcohols of liquid phase and the CO of gas phase
2, the alcohols of liquid phase imports described liquid alcohol storage tanks.
12. continous way systems as claimed in claim 11, wherein, this continous way system also comprises one second condenser, is arranged at described the second gas-liquid separation groove and described CO
2between storage tank, in order to by the CO of gas phase
2condensation imports described CO
2storage tank.
13. 1 kinds of continous way methods of preparing biofuel, comprise the following steps:
A, liquid towards alcohol pressurize and are heated to subcritical state or high-pressure liquid; Subcritical state refers to that temperature maintains lower than 240 ℃ of critical temperatures and pressure higher than emergent pressure 80atm; High-pressure liquid refers to that temperature maintains lower than 240 ℃ of critical temperatures and pressure lower than emergent pressure 80atm;
B, utilize a continous way extraction module to carry out continuous extraction, wherein this continous way extraction module has most extraction tanks, and described extraction tank is in order to receive subcritical state or high-pressure liquid alcohol, and the glyceride stock in extraction tank is extracted, to obtain extraction product;
C, extraction product is carried out to transesterification, to obtain turning esterification products; And
D, separation turn esterification products, to obtain biofuel.
14. continous way methods as claimed in claim 13, wherein, in step b, described continous way extraction module comprises three extraction tanks, in order to carry out respectively the alternately operating of glyceride stock filling, extraction and blowdown.
15. continous way methods as claimed in claim 14, wherein, in step b, described glyceride stock is the material plant that is rich in triglyceride, extraction product is triglyceride and alcohol.
16. continous way methods as claimed in claim 13, wherein, after step b, the method also comprises a heating steps, in order to heat extraction product.
17. continous way methods as claimed in claim 13, wherein, in step c, are maintained at above-critical state operational condition and carry out transesterification.
18. continous way methods as claimed in claim 13, wherein, in steps d, the fatty acid ester that is liquid phase by transesterification product separation, glycerine, and the alcohols of gas phase.
19. continous way methods as claimed in claim 18, wherein, after steps d, the method also comprises a condensing steps, in order to by the alcohols condensation of gas phase.
20. continous way methods as claimed in claim 13, wherein, before step c, the method also comprises that one provides CO
2step, it comprises condensation CO
2for liquid step, liquid CO pressurizes
2step and heat liquid CO
2and the step of extraction product.
21. continous way methods as claimed in claim 20, wherein, in step c, transesterification extraction product and CO
2, to obtain turning esterification products.
22. continous way methods as claimed in claim 21, wherein, in steps d, comprise one first gas-liquid separation step, in order to separation, turn fatty acid ester, the glycerine that esterification products is liquid phase, and the alcohols of gas phase and CO
2.
23. continous way methods as claimed in claim 22, wherein, in steps d, the method also comprises one second gas-liquid separation step, in order to receive alcohols and the CO of gas phase
2, be separated into the alcohols of liquid phase and the CO of gas phase
2.
24. continous way methods as claimed in claim 23 wherein, separately comprise a condensing steps after the second gas-liquid separation step, in order to by the CO of gas phase
2condensation.
Priority Applications (1)
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|---|---|---|---|
| CN200910262781.0A CN102108319B (en) | 2009-12-28 | 2009-12-28 | Continuous system and method for preparing biodiesel |
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|---|---|---|---|
| CN200910262781.0A CN102108319B (en) | 2009-12-28 | 2009-12-28 | Continuous system and method for preparing biodiesel |
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| CN102108319A CN102108319A (en) | 2011-06-29 |
| CN102108319B true CN102108319B (en) | 2014-02-19 |
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