CN102108319A - Continuous system and method for preparing biodiesel - Google Patents
Continuous system and method for preparing biodiesel Download PDFInfo
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- CN102108319A CN102108319A CN2009102627810A CN200910262781A CN102108319A CN 102108319 A CN102108319 A CN 102108319A CN 2009102627810 A CN2009102627810 A CN 2009102627810A CN 200910262781 A CN200910262781 A CN 200910262781A CN 102108319 A CN102108319 A CN 102108319A
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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 in detail, is the continous way system and method for preparing biofuel about a kind of relevant for a kind of system and method for preparing biofuel.
Background technology
Traditional biological diesel oil (biodiesel) is to finish with alkali technology or sour technology, but because of needs use soda acid catalyst or reactant, often causes the puzzlement of back segment purifying products and recycling.Present legal biofuel factory all belongs to first-generation technology and based on U.S.'s rule, reaction time of esterification is long, transformation efficiency is not high, because use acid and alkali raw material, liquid waste disposal is a big problem, again impurity (as saponified) that contain more, must rectifying just can reach industrial standards, cost is higher.
At present several technology of improving traditional biological diesel oil method is arranged also, two-stage transesterification technology of preparing is wherein a kind of, but also has many shortcomings; In addition,, biological transesterificationization can directly transform advantages such as free fatty acids and glycerine is easily separated though having, owing to use biocatalyzer thereby cost higher, and speed of reaction is slower; Inquire at document as for solid-state catalyst method is still many at present, the industrialization actual achievement is not arranged as yet.
United States Patent (USP) the 6th, 211,390 B1 numbers, patent name is " Method for producing fattyacid " (a fatty acid ester manufacture method), disclose a kind of supercritical extraction that utilizes and prepared method of bio-diesel oil, this patent is to be rich in the raw material of triglyceride, under the alkaline catalyst effect, carry out transesterification with alcohols, the intact excessive alcohols reactant of fatty acid ester that generates and unreacted, under the out-phase catalysis, carry out extracting and separating via near or supercutical fluid again, obtain highly purified biofuel.This patent shortcoming is to limit to some extent making biodiesel raw material, can't be widely used in the oil sources of moisture or free fatty acids; Moreover reactant methanol need in the transesterification process are excessive, carry out methanol extraction with supercutical fluid under the out-phase catalysis and separate, and may need to consume a large amount of energy and can reach the purpose of high score from purifying.
No. 466271 patent of TaiWan, China patent announcement, title " is made the method for effective for treatment of premature ejaculation " from lipid, disclosed a kind of metal base catalyst or sour catalyst of need not using, and transesterificationization prepares method of bio-diesel oil under overcritical lower alcohol state.This patent is to use lipid raw material and the reaction of low-carbon (LC) alcohols that contains free fatty acids, and Witepsol W-S 55 contained in the lipid carried out transesterification to make effective for treatment of premature ejaculation under overcritical alcohols state, simultaneously owing under the condition of not using metal base catalyst, sour catalyst, react, can not need to carry out pre-treatment step with the free fatty acids esterification, and can not generate the by product of fatty acid soaps, thereby can omit or simplify the recovery purification step of resultant.This patent only limits to make with supercritical methanol the method for effective for treatment of premature ejaculation, and raw material may be waste edible oil or biomass grease.
Point out in " Semen Brassicae campestris and supercritical methanol original position extraction-transesterification prepare biofuel " document of the 23rd the 12nd phase of volume of China's " applied chemistry periodical ": 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 greasy percentage extraction in the 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 extraction of the supercritical methanol technology of Vegetable oil lipoprotein, studying more at present is supercritical CO
2Extraction process, the document adopt the supercritical methanol method to carry out greasy extraction and supercritical extraction and overcritical transesterification reaction are combined the research for preparing biofuel all do not have reported in literature at present.Yet best extraction is also inequality with pressure condition with the service temperature of transesterificationization, and carries out supercritical extraction simultaneously and overcritical transesterification turns to batch operation in same reactor, and can't 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 extraction and overcritical alcohols transesterificationization, prepare biofuel, have the advantages that technology is simple, cost is low.
For achieving the above object, the present invention at first provides a kind of continous way system for preparing biofuel, comprising:
One liquid alcohol storage tanks is in order to storing liquid alcohol;
One continous way extraction module has most extraction tanks, and described extraction tank is in order to receiving liquid alcohol, and the glyceride stock in the extraction tank is extracted, and obtaining extraction product, and reaches continuous extraction;
One tubular type transesterification device in order to receive extraction product, carry out transesterificationization, obtains the transesterification product; And
One first gas-liquid separation groove is in order to separate the transesterification product, 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 pressurization and heat described liquid alcohol to subcritical attitude 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 the alternately operating of glyceride stock filling, extraction and blowdown respectively.
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 the heating extraction product.More preferably, this continous way system also comprises a vacuum breaker, is arranged between described second preheater and the described continous way extraction module.
In above-mentioned continous way system, preferably, described tubular type transesterification device is maintained at the above-critical state operational condition.
In above-mentioned continous way system, preferably, the described first gas-liquid separation groove is in order to being separated into the transesterification product fatty acid ester, the glycerine of liquid phase, and the alcohols of gas phase.More preferably, this continous way system also comprises a condenser, is arranged between described first gas-liquid separation groove and the described liquid alcohol storage tanks, imports described liquid alcohol storage tanks in order to the alcohols condensation with gas phase.
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 CO
2Be condensed into liquid state, this second liquid pump is with liquid CO
2Add this second preheater, this second preheater is in order to 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,, obtain the transesterification product carry out transesterificationization; The described first gas-liquid separation groove reaches the alcohols and the CO of gas phase in order to the transesterification product is separated into fatty acid ester, the glycerine of liquid phase
2
In above-mentioned continous way system, preferably, this continous way system also comprises one second gas-liquid separation groove, in order to receive the 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 second gas-liquid separation groove and described CO
2Between the storage tank, in order to CO with gas phase
2Condensation imports described CO
2Storage tank.
The present invention also provides a kind of continous way method for preparing biofuel, may further comprise the steps:
(a) liquid towards alcohol pressurizes and is heated to subcritical attitude or high-pressure liquid;
(b) utilize 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 receiving subcritical attitude or high-pressure liquid alcohol, and the glyceride stock in the extraction tank is extracted, to obtain extraction product;
(c) extraction product carry out transesterificationization, to obtain the transesterification product; And
(d) separate the transesterification product, 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 the alternately operating of glyceride stock filling, extraction and blowdown respectively.
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), this method also comprises a heating steps, in order to the heating extraction product.
In above-mentioned continous way method, preferably, in step (c), be maintained at the above-critical state operational condition and carry out transesterificationization.
In above-mentioned continous way method, preferably, in step (d), the transesterification product is separated into fatty acid ester, the glycerine of liquid phase, and the alcohols of gas phase.
In above-mentioned continous way method, preferably, after step (d), this method also comprises a condensing steps, in order to the alcohols condensation with gas phase.
In above-mentioned continous way method, preferably, (c) is preceding in step, and this method comprises that also one provides CO
2Step, it comprises condensation CO
2For the step of liquid state, 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 the transesterification product.
In above-mentioned continous way method, preferably, in step (d), comprise one first gas-liquid separation step, be fatty acid ester, the glycerine of liquid phase in order to separate the transesterification product, and the alcohols and the CO of gas phase
2
In above-mentioned continous way method, preferably, in step (d), this method also comprises one second gas-liquid separation step, in order to receive the 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, comprise a condensing steps in addition, in order to CO with gas phase
2Condensation.
The invention provides a kind of continous way system for preparing biofuel, comprising: a liquid alcohol storage tanks, a continous way extraction module, a tubular type transesterification device and 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 one of them extraction tank is in order to receiving liquid alcohol at least, and the glyceride stock in the extraction tank is extracted, and obtaining extraction product, and reaches continuous extraction.This tubular type transesterification device carry out transesterificationization, obtains the transesterification product in order to receive extraction product.This first gas-liquid separation groove is in order to separate the transesterification product, to obtain biofuel.
The present invention provides a kind of continous way method for preparing biofuel in addition, may further comprise the steps: (a) pressurization and heating liquid alcohol are to subcritical attitude or high-pressure liquid; (b) utilize 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 receiving subcritical attitude or high-pressure liquid alcohol, and the glyceride stock in the extraction tank is extracted, to obtain extraction product; (c) extraction product carry out transesterificationization, to obtain the transesterification product; Reach and (d) separate the transesterification product, to obtain biofuel.
The continous way system and method that the present invention prepares biofuel utilizes subcritical attitude or high-pressure liquid alcohols oil and grease extracting and prepares biofuel with overcritical alcohols transesterificationization, and extract via continous way extraction module and method, carry out overcritical alcohols transesterificationization again, adopt identical alcohols to extract and the transesterification program in the system and method simultaneously, can simplify technology, save the manpower and the energy.
Description of drawings
Fig. 1 shows the synoptic diagram of the continous way system of the preparation biofuel that the embodiment of the invention 1 provides;
Fig. 2 shows the synoptic diagram of the continous way system of the preparation biofuel that the embodiment of the invention 2 provides.
The primary clustering nomenclature:
The continous way system 10 of the embodiment of the invention 1 preparation biofuel; Liquid alcohol storage tanks 11;
The first liquid pump, 12; First preheater, 13; Continous way extraction module, 14; Vacuum breaker 15;
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 invention 2 preparation biofuel;
Liquid alcohol storage tanks, 31; The first liquid pump, 32; First preheater, 33;
Continous way extraction module, 34; Vacuum breaker, 35; CO
2Storage tank, 36; First condenser, 37;
The second liquid pump, 38; Second preheater, 39; Tubular type transesterification device, 40;
The first gas-liquid separation groove, 41; The second gas-liquid separation groove, 42; Second condenser, 43;
First extraction tank, 141; Second extraction tank, 142; The 3rd extraction tank, 143;
First extraction tank, 341; Second extraction tank, 342; The 3rd extraction tank, 343.
Embodiment
Embodiment 1
With reference to figure 1, it shows the synoptic diagram of the continous way system of the preparation biofuel that the embodiment of the invention 1 provides.Below utilize Fig. 1 that the continous way system and method for the preparation biofuel that the embodiment of the invention 1 provides is described.The continous way system 10 of the preparation biofuel that the embodiment of the invention 1 provides comprises: a liquid alcohol storage tanks 11, a continous way extraction module 14, a tubular type transesterification device 17 and 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 comprises one first liquid pump 12 and one first preheater 13 in addition, in order to liquid alcohol is pressurizeed and be heated to subcritical attitude or high-pressure liquid.Wherein, subcritical attitude is meant that 240 ℃ of temperature maintenance subcritical temperature and pressure are higher than emergent pressure 80atm; High-pressure liquid is meant 240 ℃ of temperature maintenance subcritical temperature and pressure subcritical 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 attitude 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 receiving liquid alcohol, and the glyceride stock in the extraction tank is extracted, and obtaining 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 the alternately operating of glyceride stock filling, extraction and blowdown respectively.Preferably, these extraction tanks are the high pressure extraction groove.
Illustrate, when carrying out the glyceride stock filling as if first extraction tank 141, second extraction tank 142 can extract, and at this moment, the liquid alcohol of subcritical attitude or high-pressure liquid imports second extraction tank 142 and extracts, and the 3rd extraction tank 143 can carry out the blowdown operation.After 142 extractions of second extraction tank finish, because the filling of first extraction tank, 141 glyceride stocks is finished, the liquid alcohol of subcritical attitude or high-pressure liquid can be imported 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 the alternately operating of glyceride stock filling, extraction and blowdown respectively, make that the extraction operation is uninterrupted continuously.
In the present embodiment, this glyceride stock is the material plant that is rich in triglyceride, for example crush to the crazy seed particle of 1-5mm granular size De Ma, this liquid alcohol is selected methyl alcohol, because of subcritical attitude methyl alcohol has splendid diffusion, matter passes and dissolving triglyceride ability, sustainable about 0.5-2hr of extraction time.So carry out oil extraction with subcritical attitude/high-pressure liquid alcohol, have productive rate height, time weak point, the advantage that optimum extraction conditions such as pressure and temperature are easy to control.If oil plant raw material rich cellulose, in high pressure, being heated is lower than 150 ℃, Mierocrystalline cellulose is not changed; High pressure, being heated is higher than the coking of can dewatering of 150 ℃ of Mierocrystalline celluloses, but for the extraction of triglyceride with continue the transesterification did not influence.Therefore, the continous way system 10 spendable raw materials of preparation biofuel provided by the invention are wide, can contain large quantity of moisture, triglyceride and free fatty acids, and raw material does not need complete drying to handle.
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 comprises a vacuum breaker 15 and one second preheater 16 in addition.This vacuum breaker 15 is arranged between this second preheater 16 and this continous way extraction module 14.Second preheater 16 makes the extraction product temperature be higher than the methanol critical temperature in order to the heating extraction product.
This tubular type transesterification device 17 carry out transesterificationization, obtains the transesterification product in order to receive extraction product.In the present embodiment, this tubular type transesterification device 17 is to be maintained at the above-critical state operational condition, carries out the supercritical methanol transesterification, and the suitableeest transesterification condition can be: service temperature is controlled to be 240 ℃-320 ℃, working pressure and is controlled to be 100-250atm.The transesterification product 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 carries out transesterificationization with supercritical alcohols and prepares biofuel, and transformation efficiency is higher, the reaction times is short, do not use the soda acid catalyst, no soda acid is handled problems again.
This first gas-liquid separation groove 18 is in order to separate the transesterification product, to obtain biofuel.The fatty acid ester (biofuel) that these first gas-liquid separation groove, 18 separation transesterification products are liquid phase, glycerine are to bottom land, and alcohols to the groove of gas phase pushes up.The continous way system 10 of preparation biofuel provided by the invention comprises a condenser 19 in addition, is arranged between this first gas-liquid separation groove 18 and this liquid alcohol storage tanks 11, imports this liquid alcohol storage tanks 11 in order to the alcohols condensation with gas phase and reclaims use.
The continous way system 10 of the preparation biofuel that the embodiment of the invention 1 provides utilizes subcritical attitude or high-pressure liquid alcohols oil and grease extracting and prepares biofuel with overcritical alcohols transesterificationization, and extract via continous way extraction module and method, carry out overcritical alcohols transesterificationization again, adopt identical alcohols to extract and the transesterification program in the system and method simultaneously, can simplify technology, save the manpower and the energy.
Embodiment 2
With reference to figure 2, it shows the synoptic diagram of the continous way system of the preparation biofuel that the embodiment of the invention 2 provides.The continous way system 30 of the preparation biofuel that the embodiment of the invention 2 provides comprises: a liquid alcohol storage tanks 31, one first liquid pump 32, one first preheater 33, 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.
Liquid alcohol storage tanks 31, the first liquid pump 32 of the continous way system 30 of the preparation biofuel that the embodiment of the invention 2 provides, first preheater 33, continous way extraction module 34 and vacuum breaker 35 are identical with the continous way system 10 of the preparation biofuel that the embodiment of the invention 1 provides, and continous way extraction module 34 has first extraction tank 341, second extraction tank 342 and the 3rd extraction tank 343, no longer narration.
In the present embodiment, before extraction product imports second preheater 39, add The addition of C O
2This CO wherein
2 Storage tank 36 is in order to store CO
2, this first condenser 37 is in order to CO
2Be condensed into liquid state, this second liquid pump 38 is with liquid CO
2Add this second preheater 39, this second preheater 39 receives liquid CO
2And extraction product, in order to liquid CO
2And extraction product heating.
This tubular type transesterification device 40 is in order to receive extraction product and CO
2,, obtain the transesterification product carry out transesterificationization.In the present embodiment, this tubular type transesterification device 40 also is maintained at the above-critical state operational condition, carries out the supercritical methanol transesterification, but because of adding CO
2The temperature and the pressure of transesterificationization are reduced, to save electric energy.And because of adding CO
2, the transesterification product comprises: fatty acid ester (biofuel), glycerine (byproduct) and the aqueous solution and unreacted methanol and CO
2
This first gas-liquid separation groove 41 is fatty acid ester, the glycerine of liquid phase in order to separate the transesterification product, and the alcohols and the CO of gas phase
2This second gas-liquid separation groove 42 is in order to receive the 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 the storage tank 36, in order to CO with 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 attitude or high-pressure liquid alcohols oil and grease extracting and prepares biofuel with overcritical alcohols transesterificationization, and extract via continous way extraction module and method, carry out overcritical alcohols transesterificationization again, adopt identical alcohols to extract and the transesterification program in the system and method simultaneously, can simplify technology, save the manpower and the energy.
The foregoing description only is explanation principle of the present invention and effect thereof, and unrestricted the present invention.Therefore, practise the foregoing description being made amendment and changing and still do not take off spirit of the present invention in the personage of this technology.The claim scope is listed as described later for interest field of the present invention.
Claims (26)
1. continous way system for preparing biofuel comprises:
One liquid alcohol storage tanks is in order to storing liquid alcohol;
One continous way extraction module has most extraction tanks, and described extraction tank is in order to receiving liquid alcohol, and the glyceride stock in the extraction tank is extracted, and obtaining extraction product, and reaches continuous extraction;
One tubular type transesterification device in order to receive extraction product, carry out transesterificationization, obtains the transesterification product; And
One first gas-liquid separation groove is in order to separate the transesterification product, to obtain biofuel.
2. continous way as claimed in claim 1 system, wherein, this continous way system also comprises one first liquid pump and one first preheater, in order to pressurization and heat described liquid alcohol to subcritical attitude or high-pressure liquid.
3. continous way as claimed in claim 1 system, wherein, described continous way extraction module comprises three extraction tanks, in order to carry out the alternately operating of glyceride stock filling, extraction and blowdown respectively.
4. continous way as claimed in claim 3 system, wherein, described glyceride stock is the material plant that is rich in triglyceride, extraction product is triglyceride and alcohol.
5. continous way as claimed in claim 1 system, wherein, this continous way system also comprises one second preheater, in order to the heating extraction product.
6. continous way as claimed in claim 5 system, wherein, this continous way system also comprises a vacuum breaker, is arranged between described second preheater and the described continous way extraction module.
7. continous way as claimed in claim 1 system, wherein, described tubular type transesterification device is maintained at the above-critical state operational condition.
8. continous way as claimed in claim 1 system, wherein, the described first gas-liquid separation groove is in order to being separated into the transesterification product fatty acid ester, the glycerine of liquid phase, and the alcohols of gas phase.
9. continous way as claimed in claim 8 system, wherein, this continous way system also comprises a condenser, is arranged between described first gas-liquid separation groove and the described liquid alcohol storage tanks, imports described liquid alcohol storage tanks in order to the alcohols condensation with gas phase.
10. continous way as claimed in claim 1 system, 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 CO
2Be condensed into liquid state, this second liquid pump is with liquid CO
2Add this second preheater, this second preheater is in order to liquid CO
2And extraction product heating.
11. continous way as claimed in claim 10 system, wherein, described tubular type transesterification device is in order to receive extraction product and CO
2,, obtain the transesterification product carry out transesterificationization.
12. continous way as claimed in claim 11 system, wherein, the described first gas-liquid separation groove is in order to being separated into the transesterification product fatty acid ester, the glycerine of liquid phase, and the alcohols and the CO of gas phase
2
13. continous way as claimed in claim 12 system, wherein, this continous way system also comprises one second gas-liquid separation groove, in order to receive the 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.
14. continous way as claimed in claim 13 system, wherein, this continous way system also comprises one second condenser, is arranged at described second gas-liquid separation groove and described CO
2Between the storage tank, in order to CO with gas phase
2Condensation imports described CO
2Storage tank.
15. a continous way method for preparing biofuel may further comprise the steps:
A, liquid towards alcohol pressurize and are heated to subcritical attitude or high-pressure liquid;
B, utilize 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 receiving subcritical attitude or high-pressure liquid alcohol, and the glyceride stock in the extraction tank is extracted, to obtain extraction product;
C, extraction product carry out transesterificationization, to obtain the transesterification product; And
D, separation transesterification product are to obtain biofuel.
16. continous way method as claimed in claim 15, wherein, in step b, described continous way extraction module comprises three extraction tanks, in order to carry out the alternately operating of glyceride stock filling, extraction and blowdown respectively.
17. continous way method as claimed in claim 16, wherein, in step b, described glyceride stock is the material plant that is rich in triglyceride, and extraction product is triglyceride and alcohol.
18. continous way method as claimed in claim 15, wherein, behind step b, this method also comprises a heating steps, in order to the heating extraction product.
19. continous way method as claimed in claim 15 wherein, in step c, is maintained at the above-critical state operational condition and carry out transesterificationization.
20. continous way method as claimed in claim 15 wherein, in steps d, is separated into fatty acid ester, the glycerine of liquid phase with the transesterification product, and the alcohols of gas phase.
21. continous way method as claimed in claim 20, wherein, after steps d, this method also comprises a condensing steps, in order to the alcohols condensation with gas phase.
22. continous way method as claimed in claim 15, wherein, before step c, this method comprises that also one provides CO
2Step, it comprises condensation CO
2For the step of liquid state, liquid CO pressurizes
2Step and heat liquid CO
2And the step of extraction product.
23. continous way method as claimed in claim 22, wherein, in step c, transesterification extraction product and CO
2, to obtain the transesterification product.
24. continous way method as claimed in claim 23 wherein, in steps d, comprises one first gas-liquid separation step, is fatty acid ester, the glycerine of liquid phase in order to separate the transesterification product, and the alcohols and the CO of gas phase
2
25. continous way method as claimed in claim 24, wherein, in steps d, this method also comprises one second gas-liquid separation step, in order to receive the alcohols and the CO of gas phase
2, be separated into the alcohols of liquid phase and the CO of gas phase
2
26. continous way method as claimed in claim 25 wherein, comprises a condensing steps, in addition in order to the CO with gas phase after the second gas-liquid separation step
2Condensation.
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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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| CN102108319B CN102108319B (en) | 2014-02-19 |
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