TW201113365A - Continuous high temperature trans-esterification process using oscillatory flow reactors for the production of biodiesel - Google Patents

Abstract

This invention is a continuous high temperature trans-esterification process, using oscillatory continuous flow reactors, for the production of biodiesel. Accordingly, one aspect of the present invention provides a continuous process for the trans-esterification of triglycerides and low carbon alkyl alcohol in a series of oscillatory continuous flow reactors, operated at a temperature higher than normal boiling point of the said low carbon alkyl alcohol. The trans-esterification reaction will be carried out in a series of oscillatory continuous flow reactors to produce biodiesel and glycerin. Glycerin and alcohol mixture will be separated from the product stream from said oscillatory continuous flow reactors by using centrifugal separators. The low alkyl alcohol and catalyst will be recovered from the said mixture of glycerin and alcohol from the first reactor by distillation. The remaining glycerin will be further purified to produce industrial grad or medical grad glycerin. Biodiesel produced from the last reactor will be washed, and evaporated to produce biodiesel product. The mixture of glycerin and low alkyl alcohol from the reactor will be sent to the previous reactor for further reaction to minimize the consumption of low alkyl alcohol.

Description

201113365 VI. Description of the invention: [Technical field to which the invention belongs] This method is a method for producing biodiesel by transesterification reaction under high temperature conditions using a reciprocating tubular continuous reactor, which is a sour acid ester As a raw material, a method of producing biodiesel by using a series of continuous reaction 'intermediate product continuous separation method and continuous conversion reaction with a basic catalyst' is employed. [Prior Art] The basic reaction of Shimumu Oil is called transesterification, that is, each planting fat i such as soybean oil (yellow soybean oil), corn oil, sunflower oil, vegetable oil, rice bran oil, palm oil, coconut oil , cottonseed oil, etc., or dynamic fat, recycled oil as a raw material 'mixed with alcohol (methanol, ethanol, propanol) and catalyst 磐, will produce a turnaround, and produce biodiesel and glycerol. The transesterification reaction may be carried out by using H, K0H or sodium decoxide as a catalyst, and the transesterification reaction is a reaction, and a batch stirring reactor is generally used and a basic contact reaction is added. This chemical reaction was first seen in the palm oil trans-vagination patent [#422,877] obtained in 1937 in QChavanne, Belgium. 3 批次 batch or continuous transfer from the natural reaction to produce biodiesel = process diagram; usually put fatty acid glyceride 21, sterol 2 〇 and ^ in the first reactor 1, from room temperature to 40 ° c to 60 Under one-degree conditions (the atmospheric boiling point of sterol is 64/rc), the reaction is stirred. ϋ Leisure: ΐ 'Standing separation or _ separator 4 separates biodiesel and glycerol by gravity separation. Then, the biodiesel cigarette is not washed in the oil washer 23, and then the water and the sterol 24 are removed from the biodiesel 14, that is, the bio-chasis ασ 5′ glycerol is used to remove the methanol 29 from the falling film evaporator 17 . In addition to 201113365, the glycerin product 31 is removed under reduced pressure in the glycerin evaporative dryer 18. Eff. 2 is 6 "rc, in order to avoid the large amount of methanol volatilization caused by the ° or the continuous reaction method is usually operated in such as C, V, shortcomings, slow reaction rate, low conversion rate, poor product, and susceptible raw materials. The quality of the oil 盥 free of the impact of the monthly acidity, making the product quality relatively unstable? 3 ί, in the reaction - for a period of time i, will make the object gradually increase, the reaction rate will soon become slow, because

The result of transesterification with methanol is that the final product will usually contain _% to Q; the biological read f has a higher conversion rate; but because of the gluten product, the glycerin product usually contains a very high/agricultural level. _, so that glycerin purely to make energy. The troubles of the rushing diesel process have proposed a favorable two-way reaction? The high temperature and high pressure τ is used to catalyze the 'handle field method to increase the reaction rate and conversion rate, and the red A _ to meet the energy requirements for glycerol purification. [Inventive content] The production method, the reactor is in Gaoqinger ^Hi 201113365, the reaction is to mix the fatty acid glyceride and other fat raw materials with the catalyst, and the reaction liquid is stirred and mixed into a single run. The pupa-transesterification reaction is carried out, and the hydrazine is continuously extracted in the course of the reaction, and purified by the biodiesel purification process, respectively, to produce biodiesel and §=来^, _ multi-stage continuous Trans-acetated biodiesel raw ί tandem-aged complex tubular continuous reactor, two should be mixed with glycerol thieves _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ Under the operating pressure, the mixture is stirred and mixed for transesterification; the multi-stage ί mi diesel production method consists of two to three reciprocating tube-type continuous processes and uses a separator to continuously glycerol and matter, 'the first reciprocating type The type of glycerol separated by the tube type, 'reverse (4)-continuous separator, directly purified to produce by-product glycerin, and the glycerol and low-alkanol separated by the continuous separator of the subsequent reciprocating ^ifi 5 Have a better Concentration of lower alkanol, therefore, is returned to the previous reciprocating continuous reactor as a reactant to save the amount of low alcohol used in the whole process and reduce low carbon burn 5 and glycerol Purify the required energy filaments. The biodiesel (such as fatty acid oxime ester, fatty acid ethyl ester or fatty acid propyl ester) produced by the final reaction is separated and purified to become a southern concentration biodiesel. [Embodiment] 201113365 The specific embodiment of the multi-stage continuous transesterification biodiesel production method of the present invention can be divided into a two-stage continuous reaction mode and a three-stage continuous g-type reaction mode as a simplified method for explaining ❶ and two stages. Continuous reaction; ^ The single-reactor mode of the transesterification method has the problem that the reactor volume is too large, the scramble effect is not easy to control, the product conversion rate is low, and the glycerin contains excessive low-carbon alcohol.

Nowadays, in order to effectively shorten the time required for transacetalization to achieve high conversion efficiency and high purity products, the method of the present invention divides the transesterification reaction into a continuous reactor of the 彳+-tube type, and combines them into The two-stage reaction mode is shown in Fig. 3, which comprises a first-stage continuous transesterification reaction and a second-stage continuous transesterification reaction, which basically transfers the fatty acid glyceride or free fatty acid raw material 21 through fat exchange. Heat n to between 60 C and 120 C, low-carbon alcohol 2 〇 (such as methanol, ethanol, propanol, isopropanol or a mixture thereof) and alkaline catalyst 19 (such as potassium hydroxide or sodium hydroxide) Preheating through a lower alkanol heat exchanger to 6 ° C 120 ° C 'in the first continuous, continuous reaction n 丨 and the second continuous reaction ^ ^ pressure 0 atmospheric pressure to 30 atmospheres, reaction ^ The transacetalization reaction is carried out using a reciprocating continuous reactor under the conditions of a temperature between 50 C and 120 C and below the boiling point of the lower alkanol. Continued reaction ΐ1 low carbon cylinder in the feed and fatty acid glycerol 酉曰, free fatty acid and other oil raw materials molar ratio of 3:1 to 3 〇:1. In addition, the amount of the test catalyst added in the device 1 is 01% to 1% by weight of the raw material of the glycerol or free fatty acid. The first continuous reactor 1 adopts a reciprocating tubular continuous reaction for the reactants and the catalyst to fully satisfy the reaction to achieve the reaction. 7 201113365 The residence time should be based on the quality of the raw materials. For five minutes to: ί ft off-separator, telecentric separator, liquid cyclone separation more than 3 segments t ^ 'parts after the first - heat exchange 7 heating, Φ ^ I ^ to enhance the transesterification of free fatty acids and fatty acid glycerides The alpha-light fraction contains the reactants and the biodiesel in the first 2 reactor 2 using a reciprocating continuous reactor; rpm = ί - in the second continuous reactor 2, the first exiting organism Diesel and incompletely reacted J J 2; ^ (Ϊ Ϊ 3 3 醇 醇 醇 醇 醇 或其 或其 或其 或其 或其 与 或 或 或 或 或 ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; ; Under the condition of low-carbon hospital alcoholic spot, the transesterification reaction is carried out by using a hydrazine double-type continuous reactor. The molar ratio of low-carbon alcohols and fatty acid hydrazines such as fatty acid hydrazine or fatty acid is continuously added in the reactor 2. 3:1 to the type of anti-filament 2 added to the secret touch county added amount of lunar i-glyceride or free fat 01% to 1% by weight of the raw material. ί ϊΐί ί 2 uses a reciprocating tubular continuous reactor domain reactant and fully agitated to fully mix the reactants with 201113365; the reaction of the first reaction H I and degree f force it reaction residence time is usually iSs, 20 knife buckle. The second continuous reactor 2 product uses the second process, the separation of H 5 to separate, gravity sedimentation separator, remote, A liquid cyclone separator or a multi-stage liquid cyclone separator, etc., the glycerin and low-carbon alcohol in the reaction product are extracted and the telecentric separator is most efficient; the second continuous crying/, "light biomass biodiesel" With the incomplete reaction, i, $ 1 part? 2 continuous reactor 2, to improve the conversion efficiency of the catalyst transesterification; the remaining masses are mixed to the biodiesel g, sent to the sodium salt tower 33 i = The biodiesel after washing in the biodiesel washing (4) 13 is then dried by biodiesel. The condenser is condensed and removed, and the olefin is obtained as a retort or liquid membrane evaporator. dry

ί ί type separator 4 / separated glycerol and lower alkanol, add neutralizer 26 in ΐΐ m, separate *resource production it, and then remove the low sulphur alcohol in the glycerol falling film = Qiao After that, send it to r-alcohol _ pull 3 two' will be used. The second detachment = glycerin after the scale is broken ‘201113365 for wastewater 22. Since glycerol has a high boiling point, glycerin evaporative dryers are usually operated at a vacuum of less than 2 atmospheres. The glycerol evaporative dryer is a distillation column or a liquid film evaporator. Three-stage continuous reaction mode & In order to further shorten the time required for the transesterification reaction and to treat the deteriorated fat and free fatty acid to achieve high conversion efficiency and high purity product, the present invention further develops the reaction method into a reactor having a small volume. A high-temperature three-stage continuous transesterification method with a fast reaction rate and a high conversion rate, and a three-stage continuous reaction mode formed by using a continuous reactor, as shown in Fig. 4, which includes the first continuous transesterification reaction, The second-stage f-transesterification reaction and the third-stage continuous transesterification reaction basically carry out the fatty acid glyceride or free fatty acid raw material 21 through the grease heat, and the converter is advanced to 60. 〇 to 120 ° C, low carbon alcohol 20 (such as, A, diethanol, propanol, isopropanol or a mixture thereof) and alkaline catalyst 19 (such as sodium, potassium hydroxide or sodium sulfoxide) First, the low-alkanol is heat-crossed between jc and 120 ° C, in the first continuous reactor 2 and the third continuous reactor 3, at a pressure of 3 to 3 atm, and the reaction temperature is below, and the Add 201113365 Ϊ 2: ί2 ίί 丄 丄 进行 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 丄 反应 反应 反应The first continuous 1 i, the product uses the first continuous separator 4 to separate the liquid separation tank, the core separator, the liquid cyclone separation Hi multi-i type, the wind separation crucible and other mechanical methods are continuous The reaction is produced; and = alkane, which, in turn, uses a telecentric separator: ϊί 佳 , the biodiesel separated from the first continuous separator 4 and the untreated product, partially pre-treated by the first heat exchanger 7 The heat is sent back to the continuous reactor 1 to increase the conversion efficiency of the transesterification reaction; the reaction is not completely recorded and then reacted in the second reactor. The molar ratio of the low-carbon alcohol alcohol to the fatty acid glycerin Sg or the free sulfonic acid-specific oil and fat raw material added in the first continuous reactor 2 is 3.1 to, and the alkalinity added in the second continuous reactor 2 The catalyst is added in the amount of fatty acid glyceride or free fatty acid raw material. The second continuous reactor 2 uses a reciprocating tubular continuous reactor, and the biodiesel separated from the first continuous separator 4 The complete reaction product is further added with a lower alkanol (such as decyl alcohol, ethanol, propanol or a mixture thereof) and a catalyst (such as sodium hydroxide, potassium hydroxide or sodium methoxide), and fully stirred to reach The reaction residence time of the second continuous reactor should be determined according to the quality of the raw materials and the operating temperature, and the reaction residence time is usually five minutes to thirty minutes. The reaction product produced by the second continuous reactor 2 utilizes a second connection 11 201113365 ί ΐΐϊ 5 = a liquid separation tank, a gravity sedimentation separator, a telecentric separation tίfίΐ^ ί multi-stage liquid cyclone, etc. In addition, the glycerin and the lower alkanol in the reaction product are extracted, and the telecentric separator is the most efficient; the second continuous separator is used to test the substance, and the part is sent back, = Reactor 2, to increase the conversion of the catalyst transesterification reaction, and the incompletely reacted product is separated in the third stage in the third continuous reactor 3 using a reciprocating tube type L continuous separator 5. The biodiesel and the wangwang reaction product are then added to the low carbon house alcohol (such as methanol, ethanol, propanol 'isopropanol or a mixture thereof) and the catalyst (such as sodium hydroxide, f hydrogen or methyl oxidized sodium) , the reactor Lili is the pressure of the pressure to atmospheric pressure, the reaction temperature is 50 ° c to 12 (between TC and below the boiling point of the lower alkanol at normal pressure, fully stirred to achieve the reactant charge The purpose of mixing; the reaction retention of the third continuous reactor g should be regarded as the original The material quality and the operating temperature are determined, and the reaction lag is usually from five minutes to thirty minutes. The molar ratio of the lower alkanol and the fatty acid glyceride or free fatty acid material added in the third continuous reactor 3 is ^ 3:1 to 30:1. 'The amount of catalyst added in the third continuous reactor 3 is 重量.1% to 1% by weight of the fatty acid glyceride or free fatty acid raw material: 曰 third continuous reactor The reaction product of 3 uses a third continuous separator 6 to connect the glycerin in the reaction product by a mechanical method such as a liquid separation tank, a gravity sedimentation separator, a telecentric separator, a "a wind separator, or a multi-stage liquid cyclone. With the low-alkanol extraction, especially the combination of the 'Y, Yuan = separation efficiency is best; separated by the third continuous separator 6 12 201113365 f Chai Qiao and the part of the incomplete reactants returned to the third continuous

Should be _ efficiencies; its sub-biodiesel and traces of incomplete reactants, C ϋ ϋ ϋ ι # * degree = gas = lower = = dryer is a steam tower or liquid film evaporator. , wood / ", '1 dry, at

t from itl吏 with glycerol separator 16 low carbon 1S, sent to i alcohol nano take: in the first step will be condensed and removed, the bottom of the tower will get crude glycerin product 爿.丄 丄 , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , Glycerol Evaporation Dryer for Steaming Pavilion ί 13 201113365

Since the reaction conditions used in the method are from 50 ° C to 120 ° C, when the glycerol and the biodiesel are separated, the biodiesel will contain a trace concentration of the lower barrier alkanol and the transesterification reaction is an exothermic reaction. Therefore, the present invention further A plurality of heat exchangers are provided in each reactor, the heat exchanger 7 provides heat exchange of reactants and products of the continuous reactor 1; the heat exchanger 8 provides heat exchange of reactants and products of the continuous reactor 2; The heat exchanger 9 provides heat exchange between the reactants of the continuous reactor 3 and the product; in addition to recovering the energy of the reactants, the reaction product is reduced to facilitate the separation operation. The grease heat exchanger 11 and the lower alkanol heat exchanger 10 serve to provide preheating when the system is started. The μ device is used in the present invention, and the first continuous reactor 丨, the second continuous reactor 2, and the second continuous reactor 3 use a reciprocating tubular continuous reaction which can increase the pressure and black grip. (0FR). The first continuous separator 4 used in the present invention, the second continuous E-f continuous separator 6 can use a liquid separation tank separator, a heart separator, a liquid cyclone separator. Or multiple segments

'To achieve the purpose of separating glycerin from biodiesel; as a response to the need for production, and further to the efficiency of the telecentric separator H, the glycerin separator 16 used in the present invention and the biological separation using a vacuum separation tank or a liquid membrane evaporator, The glycerin evaporative dryer 18 and the dryer 14 which can be used in the present invention can be operated by using a distillation column, a liquid film, and biodiesel to evaporate and dry H16, usually under a vacuum of atmospheric pressure. Towel row, cooker twice 0.2 The heat exchanger 7, heat exchanger 8, heat exchanger 9, 201113365 hot parent 1 (), grease heat exchanger 11, condenser 34, aged 21 for use in the present invention The condenser 36 can use a shell-and-tube heat exchanger or a multi-stage continuous-type biodiesel production method, and the catalyst T used in the following is potassium hydroxide, sodium hydroxide or methanol. However, it is preferred to use sodium sterol. The above is only illustrative for the purposes of the present invention, and it will be understood by those of ordinary skill in the art that the invention may be made without departing from the spirit and scope of the invention. The patent scope of the present invention can be limited to [the simple description of the drawings] The biodiesel production method, the fatty acid glycerin or the fat and the fat and the lower alkanol (such as methanol, ethanol, C1) , J propanol or a mixture thereof, reacted with the contact, after the age, the production of biodiesel and glycerol; / strip sergeant, the second phase of the process of transesterification biodiesel production ... 'pattern, first After the separation reaction product is separated, it is sent to the reactor to continue the reaction, wherein in the first stage, the second f is over 2, so that the S continuous separator is continuously glycerin and charcoal ' ^ and the first stage reactor Further, a lower alkanol (such as a molar ratio of alcohol, isopropanol) and a catalyst may be added to enhance the reaction. Figure 3 is a multi-stage continuous transesterification biodiesel production method, the first paragraph After the reaction product is separated, it is sent again; The reaction is carried out; after the second stage reaction product is passed, it is sent to the second stage reactor to continue the reaction; wherein in the 15th, the glycerin is continuously used as a continuous separator reactant, as a sulphur, a private alcohol or a wei _ Catalyst, [main component symbol description]; gas?? Continued reaction 11; 2n complex tube type connection: :^^: second reciprocating tube type continuous reaction 15; 4, -j, j type continuous separator; 6_ third continuous type separator, 7- a hot parent shift; 8_ second heat exchange thin; 9_ second changer; 10-low carbon burn alcohol heat exchanger; U two oil month ^ exchanger; Ί bioseparator · ' 13_ biodiesel Washer; "1'4 · biodiesel evaporation dryer, 15-glycerin neutralization tank; 1 glycerol separator; 17_ falling film vaporizer; 18-glycerol evaporation dryer; 19_catalyst; 2 〇 _ low Carbonalkanol; 21-diglyceride clever free fatty acid; 22_ steaming waste water; 23-wash water; 24-low-burn alcohol and wash water (connected to vacuum pump); 25-biodiesel; 26-neutralization 27-resourced product; 28_low-breaking alcohol; sterol solution of melon catalyst; 30-low-carbon alcohol (connected to vacuum pump); 31-glycerol; 32-sewage; 33-sodium methoxide distillation column; 34-condenser; 35-condenser; 36-condenser.

Claims (1)

201113365 VII, the scope of application for patents ^ A high-temperature multi-stage continuous transesterification bio-Chai special; reminder = Gan fine or free fat grade oil original _ g & ^ de-temperature '= transacetation reaction, and in the reaction In the process of segmentation ίΐίϊϋ: άϊίί yeast extraction, and separately using the biodiesel secretification process for purification, to generate biodiesel The alkanol is methanol, ethyl acetate, propanol, isopropanol or a mixture thereof. 3 生围! / 斤 describes the high-temperature multi-stage continuous 旨 靡 靡; 苎 苎 production method, which is characterized by · · can be a two-stage continuous reverse 2, mode or three-stage continuous reaction mode multi-stage continuous reaction mode m. The multi-stage continuous trans-acetal bio-synthesis described in Patent Application No. 3 is characterized in that: a two-stage continuous reaction mode package: a continuous transesterification reaction and a second continuous transesterification reaction Anti-I 丄 basically preheats the heat exchanger of fatty acid such as fatty acid glyceride or free fatty acid, and the low-alkanol and the catalyst are preheated by the low-carbon alcohol changer in the first reciprocating tube type continuous type. The reactor is mixed and mixed into a single fluid phase for transesterification, and a continuous separator is used to mechanically continuously extract the low-carbon 1-carbon alcohol in the reaction product. The first continuous separator is separated and contains the beginning of life. The wood oil and the unreacted reactant are partially refluxed to the first reciprocating tube 17 201113365 continuous reactor, and the rest is further reacted in the second reciprocating tube, and then added in the second reciprocating tube Low barrier alkanol and catalyst, mixing and mixing into a single A fluid phase ί 2 Zhongku = second continuous separator with mechanical side: ==== unreacted reactant part ^^, the rest is purified by biodiesel separator biodiesel purification process, by the first The glycerol and low-carbon alcohols are then processed by the sweet and oil purification process, a. 3/kg of high-temperature multi-stage continuous vinegar turning and doubling reaction'. Basically, fatty acid glycerin, or fatty acid such as eucalyptus fatty acid is pre-twisted by oil enthalpy exchanger, and Si hydrazine is exchanged with lower alkanol. Preheating - glycerin in the iiy reaction product is withdrawn from the low carbon ride; the biodiesel separated from the first phase is reacted with the incomplete reaction product, the type is continuously reacted, and the rest is reacted in a type of reactor, and The second load! Soap II 13, the addition of low-carbon alcohol and catalyst in the continuation device, smashed: continuous vinegarization reaction; then ΐΐΐ ί oil and low carbon are still extracted and sent back to the first-reciprocating pipe type The bio-firewood separated from the second continuous separator, the second reaction product, partially refluxed to the second reciprocating tube type, the single-type reactor, and the rest is continuously continuous in the third reciprocating tube type Reactor in the reactor 201113365' and re-energize in the third reciprocating tubular continuous reactor: into the low-carbon alcohol and the catalyst, stir and mix into a single fluid phase for the brewing reaction, and use the third continuous Separator mechanically continuous production The glycerin and the lower alkanol are withdrawn and sent back to the second reciprocating continuous reactor; the third continuous separator is mechanically discharged, the biodiesel and the incompletely reacted product are partially returned to the tenth reciprocating tube type continuous type The reactor is separated from the catalyst by a biodiesel separator, and then the biodiesel is purified by a biodiesel purification process, and the first continuous separation of glycerol and low carbon The alkanol is further purified by a glycerol purification process. J 6 is a high temperature multi-stage continuous crucible according to the patent application 4 or 5, which is characterized in that the biodiesel is pure, sputum and low carbon bribes and then washed in biodiesel. ί ϊ ΐϊ ΐϊ 将 将 将 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 残留 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油 柴油The resource-derived product and crude glycerol, 201113365, the high-temperature multi-stage continuous transesterification of sodium as described in the description of the high-temperature multi-stage transesterification. The method is characterized in that the alkaline catalyst is hydrogen hydroxide. . ~ , Biodiesel is a high-temperature multi-stage continuous conversion potassium sulphate described in ίί, ί围i. The production method is characterized in that the alkaline catalyst is a high-temperature multi-stage continuous conversion sodium which is described by the oxidation. The invention is characterized in that: the alkaline catalyst is a high-temperature multi-stage continuous transesterification method according to the method described in the above, wherein the alkaline catalyst is used in a separator (2). : make _ method The high-temperature multi-stage continuous residual production method described in Patent No. 4 or 5 is characterized in that the separator using the mechanical method is a liquid separation tank. The high-temperature multi-stage continuous esterified biodiesel production method according to claim 4 or 5, characterized in that the mechanical separator is a telecentric separator. 16. The high-temperature multi-stage continuous 化^, a diesel production method according to claim 4 or 5, characterized in that the biodiesel evaporative dryer is used to separate the moisture in the biodiesel from the low-carbon alcohol. 17. The high-temperature multi-stage continuous transfer biodiesel production method according to claim 16, characterized in that the biodiesel evaporation ^201113365 dryer is a distillation column or a liquid film evaporator. 18. The high temperature multi-stage continuous transesterification biodiesel production method according to claim 16 wherein the biodiesel evaporative dryer operates at a vacuum of 0.2 atm or less. 19. The high-temperature multi-stage continuous transesterification biodiesel production method according to claim 4 or 5, characterized in that the moisture in the crude glycerin and the lower alkanol are separated by a glycerin evaporative dryer. The high-temperature multi-stage continuous transesterification bio-wood oil production method according to the invention of claim 19, characterized in that the glycerol-based hair dryer I is a distillation column or a liquid film evaporator. 21: The high-temperature multi-stage continuous transesterification and drowning diesel production method according to claim 19, wherein the glycerin evaporative dryer is operated at a vacuum of 0.2 atm or less. 25· According to the scope of application for patent 4 The high-temperature multi-stage continuous transfer t to 120〇c 5 is characterized by the reaction atmospheric pressure of the reactor, and the reaction temperature is 50 ° C. According to the high-temperature township continuous vinegar described by Shen Wei, she encircles the 21 201113365 ίΐίϊ The oil production method is characterized in that: the reaction dust of the reactor is 0 to atmospheric pressure to 15 large _, and the reaction temperature is up to loo c 〇 27. According to the high-temperature multi-stage continuous conversion described in Patent Application No. 4 or 5? The diesel production process 'is characterized in that the reactivity of the reactor is lower than the boiling point of the lower alkanol at the corresponding reaction pressure. 28. The method for producing a high-temperature multi-stage continuous transesterified oil according to the invention of claim 27, wherein the reaction temperature of the reaction 11 is lower than the boiling point of the lower-carbon oxy-alcohol corresponding to the reaction dust. 29. The high-temperature multi-stage continuous transesterification biodiesel production method according to claim 4 or 5, characterized in that the low-carbon alcohol and the fatty acid glyceride or free fatty acid in the first continuous reactor The molar ratio of the raw materials is from 3:1 to 30:1. 30. The high temperature multi-stage continuous transesterification hepta diesel production method according to claim 4 or 5, characterized in that the lower alkanol molar amount and the fatty acid glycerol are further added in the second continuous reactor The ratio of the grease molar amount such as ester or free fatty acid is 3:1 to 3〇;曰飞 31 · High temperature multi-stage continuous transesterification according to patent application 5 The method for producing oyster sauce is characterized in that the ratio of the number of moles of the lanthanide to the molar amount of the fatty acid glyceride or free fatty acid in the third continuous reactor is 3:1 to 3: 1. 32. A high temperature multi-stage continuous transesterification 2 bismuth oil production process according to the scope of the patent application ??? characterized in that the moisture content of the reactants in the first continuous reactor is less than. 33. A high temperature multi-stage continuous transesterification biodiesel production process according to claim 4 or 5, characterized in that each continuous reactor has a set of heat exchangers for providing heat of reactants and products of the reactor^ 22 201113365 3 or 5 of 9 good paragraph Lai Shi turn · = ^ 22 more, two $ pepper lies in: with grease preheating use Lai to make the job as a system 3 ί:? ί gas Shen i Qing F Li 围 1 The high-temperature multi-stage continuous conversion and bio-oil production y method is characterized in that the reciprocating tubular-type continuous reactor used has a mechanical preparation for providing a reciprocating simple harmonic motion of the fluid. " 36. A method for producing a high temperature multi-stage continuous transesterification biodiesel according to claim 1 wherein the reciprocating tubular continuous reactor used has an automatic mixing and mixing device in the tubular reactor.