CN101948383B - Device and method for preparing medium-high carbon fatty acid ester by continuous alcoholysis method - Google Patents
Device and method for preparing medium-high carbon fatty acid ester by continuous alcoholysis method Download PDFInfo
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- CN101948383B CN101948383B CN201010506974.9A CN201010506974A CN101948383B CN 101948383 B CN101948383 B CN 101948383B CN 201010506974 A CN201010506974 A CN 201010506974A CN 101948383 B CN101948383 B CN 101948383B
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Abstract
The invention discloses a device and method for preparing medium-high carbon fatty acid ester by the continuous alcoholysis method. The device comprises a tower reactor, wherein the tower reactor contains an ester discharge hole, an alcohol inlet, a fatty acid inlet and a steam outlet and also contains a grid; the grid is provided with a filler layer formed by tightly stacked filler; and the tower reactor also contains a disk-shaped atomization distributor and a coil heater. The method comprises the following steps: 1) pumping liquid alcohol with the dissolved alkali metal catalyst in the tower reactor; 2) pumping liquid lipid in a heat exchanger to heat and send to the tower reactor; 3) form a uniform film of liquid lipid on the surface of the filler; and 4) using the liquid alcohol and the lipid in the liquid film state to perform a catalytic alcoholysis reaction under the action of the alkali metal catalyst. The method of the invention has short time, high conversion rate and low energy consumption.
Description
Technical field
The present invention relates to a kind of equipment and method of preparing fatty acid ester, be specifically related to a kind of equipment and method of preparing medium high carbon fatty acid methyl ester or medium high carbon fatty-acid ethyl ester.
Background technology
The alleged medium high carbon fatty acid ester of the present invention refers to that the carbonatoms in carbochain is the fatty acid ester of 6 to 18, and medium high carbon fatty acid ester generally can be by medium high carbon lipid acid and alcohol generation esterification and made.At present, the preparation method that the typical method of the esterification of medium high carbon lipid acid is discontinuous, the method equipment used is shown in Fig. 1.Reactor a in Fig. 1 is with agitator b, and reflux exchanger c is equipped with on the top of this reactor a.While preparing medium high carbon fatty acid ester, to after medium high carbon lipid acid and the accurate proportioning of alcohol, drop in reactor a, in the chuck d of reactor a, pass into steam and make at a certain temperature material system reflux and generate the reaction of medium high carbon fatty acid ester, in reaction process, must stir on backflow limit, limit, a large amount of excessive alcohol is constantly back in reactor a by reflux exchanger c.The shortcoming of the method is: (1), due to the boiling point of alcohol lower (methyl alcohol is 64.5 DEG C, and ethanol is 78.4 DEG C), therefore back flow reaction temperature is lower, causes the reaction times longer, generally needs 6h～8h just can react completely.(2) reaction conversion ratio is not high, between 90%～95%.(3) need to ensure that esterification is complete with a large amount of alcohol, and a large amount of alcohol refluxing constantly flows into the temperature in meeting reduction reactor a in reactor a, thus necessary constantly heating maintenance temperature of reaction, and energy consumption is higher.(4) shipwreck generating in reaction process is to remove.
Summary of the invention
The object of the invention is to overcome the problems referred to above, a kind of equipment and method of preparing medium-high carbon fatty acid ester by continuous alcoholysis is provided, the method time is short, transformation efficiency is high, energy consumption is low.
The technical scheme that realizes one of the object of the invention is: a kind of equipment of preparing medium-high carbon fatty acid ester by continuous alcoholysis, comprises heat exchanger.Also comprise air film type reaction unit; Air film type reaction unit is tower reactor; This tower reactor comprises the tower main body of cylinder shelly and is separately positioned on ester discharge outlet, liquid alcohol entrance, grease entrance and the vapour outlet in tower main body from bottom to top; Ester discharge outlet is positioned at the bottom of tower main body, and liquid alcohol entrance is positioned at tower main body side subordinate side, and grease entrance is positioned at tower main body sidepiece top, and vapour outlet is positioned at the top of tower main body; The bottom of tower main body is liquid storage portion.Tower reactor also comprises the grid being fixed in tower main body; Described grid is arranged between liquid alcohol entrance and grease entrance; Grid is provided with the packing layer that the intensive filler of banking up forms.Tower reactor also comprises the dish type atomization sparger and the spiral heater that are fixed in tower main body; Spiral heater is positioned at the liquid alcohol entrance below of tower main body; Dish type atomization sparger is the coil pipe that has conventional quantity and big or small atomization spray orifice on tube wall; Dish type atomization sparger is positioned at the top of tower main body, and airtight being connected of grease entrance of its opening for feed and tower reactor.Heat exchanger is airtight being connected of grease entrance with tower reactor by its material outlet and corresponding pipeline.
Filler is ceramic Pall ring or by the Stainless Steel Cloth round shape reticulation forming of reeling.
Grid has 3 to 10 layers, is equipped with the packing layer that the intensive filler of banking up forms on every layer of grid.
The height of described tower reactor is 15～30m, and diameter is 0.5～3m; Described grease entrance to the distance at the tower main body top of cylindric tower reactor is 0.5～1.5m; Described liquid alcohol entrance to the distance of the tower bottom part body of cylindric tower reactor is 5～10m; Basecoat in described grid is positioned at described liquid alcohol entrance top 0.5～1m; The nozzle diameter of described vapour outlet is 0.1～0.5m; The loading height of described packing layer is 1～5m; Distance between the upper end of the material on the lower end of last layer grid and lower one deck grid is 20～35cm.
The technical scheme that realizes another object of the present invention is: a kind of method of preparing medium-high carbon fatty acid ester by continuous alcoholysis, has following steps: 1. continuously the excessive liquid alcohol that is dissolved with base metal catalysts in liquid alcohol storage tank is pumped into the bottom the tower main body of air film type reaction unit by the first volume pump from liquid alcohol entrance; Described alcohol is methyl alcohol or ethanol; Described base metal catalysts is KOH or NaOH; The weight of base metal catalysts accounts for 0.1～0.5% of base metal catalysts and liquid alcohol gross weight; 2. carry out step 1. in, continuously the liquid fat in insulated tank is pumped in operating heat exchanger and made it to be heated to 120 DEG C～150 DEG C by the second volume pump taking the mol ratio of grease and liquid alcohol as the ratio of 1: 5～1: 7, under the second volume pump pump pressure, grease is entered in dish type atomization sparger by the grease entrance of the material outlet of heat exchanger, corresponding pipeline and air film type reaction unit; Described grease is medium high carbon glycerin fatty acid ester, and wherein the carbonatoms of the carbochain of medium high carbon fatty acid radical is 6 to 18; 3. under the second volume pump pump pressure, liquid fat becomes vaporific drop ejection and enters in the upper cavity of tower main body after dish type atomization sparger, under action of gravity, after falling on filler, the surface along filler is carried out downward the flowing of general trend and is successively dropped down onto on the filler of lower floor more then, and in flowing the filling surface of process form uniform liquid film; 4. 1. enter under the effect of the heat that the liquid alcohol of tower main body sends at spiral heater and be vaporizated into alcohol steam and pass through continuously from bottom to top packing layer by step, thereby the catalyzed alcoholysis that this alcohol steam with the grease in liquid film state on filler generation medium high carbon fatty acid ester and glycerine occurs under the effect of base metal catalysts in each packing layer reacts; 5. the medium high carbon fatty acid ester being generated by step catalyzed alcoholysis reaction 4. and glycerine are under the effect of gravity, fall to the liquid storage portion of the bottom of the tower main body of air film type reaction unit, send in refining separating still and leave standstill by product pump through by-pass valve control again, under action of gravity, sedimentation is separated into two-layer up and down, glycerine under, medium high carbon fatty acid ester is upper; Separate glycerine from bottom, remaining medium high carbon fatty acid ester is sent into crude product storage tank; After catalyzed alcoholysis reaction, excessive alcohol steam is motion from bottom to top in the tower main body of air film type reaction unit, during through dish type atomization sparger, the space between the adjacent body of its coil pipe, pass, then rise to top and from the give vent to anger tower main body of film type reaction device of vapour outlet Continuous Flow.
Also there is following step: the medium high carbon fatty acid ester crude product 6. 5. step being obtained is refined: medium high carbon fatty acid ester crude product is sent into and in distillation tower, carried out underpressure distillation, the residual voltage of controlling in distillation tower is that 10～20mm mercury column, temperature are 250 DEG C～280 DEG C, makes medium high carbon fatty acid ester crude product become finished product by distilling; The alcohol vapour stream that step is flowed out continuously at the top of air film type reaction unit in 5. enters by corresponding pipeline in alcohol steam treatment system, by refrigerated water as heat-eliminating medium by the cooling alcohol vapour stream liquid alcohol that becomes, this liquid alcohol can be recycled.
The base metal catalysts of step in is 1. KOH.
The grease of step in 2. and the mol ratio of liquid alcohol are 1: 6.
The present invention has positive effect: (1) method of the present invention joins excessive liquid methanol or ethanol in air film type reaction unit with together with base metal catalysts in being dissolved in liquid alcohol, liquid alcohol is vaporizated into alcohol steam and in convection current, mainly carries out catalyzed alcoholysis at filling surface with liquid fat and react, greatly increase so on the one hand the contact area between reactant, thereby make on the other hand reaction carry out under comparatively high temps because the temperature of alcohol steam is higher, not only can the needed heat of rapid, high volume postreaction, and greatly accelerate speed of response, thereby shorten the reaction times, the original alcoholysis reaction time shorten of 6 to 8 hours is arrived within 10 points of kinds.(2) method of the present invention makes the fatty acid ester and the glycerine that in reaction process, produce under action of gravity, fall to the bottom of tower main body and not rest on filler or catalyst surface, thereby has greatly improved transformation efficiency, and transformation efficiency can reach more than 98%.(3) method energy consumption of the present invention is low, only has 1/10～1/20 of traditional technology.(4) method of the present invention has realized serialization production, and output can reach even hundreds of times of the decades of times of traditional technology, is applicable to scale operation.(5) fatty acid ester that prepared by method of the present invention is through purity after refining more than 99.5%.
Brief description of the drawings
Fig. 1 is the schematic diagram that traditional technology is prepared the device of fatty acid ester employing.
Fig. 2 is the schematic diagram of equipment of the present invention.
Label in above-mentioned accompanying drawing is as follows:
Reactor a, agitator b, reflux exchanger c, chuck d,
Tower reactor (air film type reaction unit) 1, tower main body 10, ester discharge outlet 11, liquid alcohol entrance 12, grease entrance 13, vapour outlet 14, liquid storage portion 15, grid 16, dish type atomization sparger 17, spiral heater 18,
Packing layer 21,
Liquid alcohol storage tank 31, the first volume pumps 33,
Insulated tank 41, the second volume pumps 42, heat exchanger 43,
Product pump 51,
Alcohol steam treatment system 6, the second heat exchangers 61, liquid alcohol buffering withdrawing can 62.
Embodiment
(embodiment 1)
The equipment of the preparing medium-high carbon fatty acid ester by continuous alcoholysis that the present embodiment adopts is shown in Fig. 2, and this equipment comprises air film type reaction unit 1, liquid alcohol storage tank 31, the first volume pump 33, insulated tank 41, the second volume pump 42, heat exchanger 43, product pump 51 and alcohol steam treatment system 6.
Air film type reaction unit 1 is tower reactor, and it is highly 27m, and diameter is 3m, and its material is 316L stainless steel.This tower reactor 1 comprises the tower main body 10 of cylinder shelly and is separately positioned on ester discharge outlet 11, liquid alcohol entrance 12, grease entrance 13 and the vapour outlet 14 in tower main body 10 from bottom to top.On ester discharge outlet 11, liquid alcohol entrance 12, grease entrance 13 and vapour outlet 14, be respectively equipped with by-pass valve control.
Ester discharge outlet 11 is positioned at the bottom of tower main body 10.Liquid alcohol entrance 12 is positioned at tower main body 10 sidepiece belows, and liquid alcohol entrance 12 to the distance of tower main body 10 bottoms is 6m.Grease entrance 13 is positioned at tower main body 10 sidepieces tops, and grease entrance 13 to the distance at tower main body 10 tops is 1m, thereby liquid alcohol entrance 12 to the distance between grease entrance 13 is 20m.Vapour outlet 14 is positioned at the top of tower main body 10, and the nozzle diameter of vapour outlet 14 is 0.3m.The bottom of tower main body 10 is the liquid storage portion 15 of depositing liquid medium high carbon fatty acid ester and glycerine.
Tower reactor 1 also comprises the dish type atomization sparger 17 and the spiral heater 18 that are fixed in tower main body 10.Spiral heater 18 is positioned at liquid alcohol entrance 12 belows of tower main body 10, and in spiral heater 18, passing into as the temperature of medium is the water vapour of 100 DEG C.Dish type atomization sparger 17 for having the coil pipe of conventional quantity and big or small atomization spray orifice on tube wall, also the structure that is atomization sparger is that the bottom on body just has every 1～5cm the disk-shaped tube that diameter is the aperture of 0.5～1.5mm, and described aperture is also atomization spray orifice.Dish type atomization sparger 17 is positioned at the top of tower main body 10, and airtight being connected of grease entrance 13 of its opening for feed and tower reactor 1.
Tower reactor 1 also comprises that being fixed on 3 to 10 layers of grid 16(the present embodiment that set gradually in tower main body 10 and according to upper and lower order is 5 layers), grid 16 is arranged between liquid alcohol entrance 12 and grease entrance 13, and its material is 316L stainless steel.On each layer of grid 16, intensive heap is equipped with filler and forms packing layer 21, and the loading height of packing layer 21 is 3m.Distance between the upper end of the material on the lower end of last layer grid 16 and lower one deck grid 16 is 25cm.
Filler in packing layer 21 is ceramic Pall ring or by the Stainless Steel Cloth round shape reticulation forming of reeling.The material of described Stainless Steel Cloth is 316L stainless steel.
Alcohol steam treatment system 6 comprises the second heat exchanger 61 and liquid alcohol buffering withdrawing can 62.The material outlet of the second heat exchanger 61 is airtight being connected of material inlet with liquid alcohol buffering withdrawing can 62 by exterior line.
Liquid alcohol storage tank 31 is airtight being connected of material inlet with the first volume pump 33 by exterior line, and the material outlet of the first volume pump 33 is airtight being connected of liquid alcohol entrance 12 with tower reactor 1 by exterior line.
The discharge port of insulated tank 41 is airtight being connected of material inlet with the second volume pump 42 by exterior line, and the material inlet of the first volume pump 33 is airtight being connected of material outlet with liquid alcohol buffering withdrawing can 62 by corresponding exterior line also; The material outlet of the second volume pump 42 is airtight being connected of material inlet with heat exchanger 43 by exterior line, and the material outlet of heat exchanger 43 is airtight being connected of grease entrance 13 with tower reactor 1 by exterior line.
The vapour outlet 14 of tower reactor 1 is the second airtight being connected of heat exchanger 61 material inlets with mixing steam treatment system 6 by exterior line.
Still see Fig. 2, the method for the preparing medium-high carbon fatty acid ester by continuous alcoholysis of the present embodiment has following steps:
1. the bottom in the continuous tower main body 10 that the excessive liquid methanol that is dissolved with base metal catalysts KOH in liquid alcohol storage tank 31 is pumped into operating air film type reaction unit 1 by the first volume pump 33.The present embodiment liquid methanol used is that KOH is dissolved in the anhydrous methanol of purity >=99.5% and is obtained, and wherein, the weight of KOH accounts for 0.3% of KOH and liquid methanol gross weight.
2. carry out step 1. in, (be medium high carbon glycerin fatty acid ester by the liquid fat in insulated tank 41 continuously, wherein the carbonatoms of the carbochain of medium high carbon fatty acid radical is 6 to 18, in different embodiment, select respectively Oleum Cocois or carbon plam oil, grease temperature is 80 DEG C) pump in operating heat exchanger 43 and make it to be heated to 120 DEG C～150 DEG C by the second volume pump 42 taking the mol ratio of grease and liquid alcohol as the ratio of 1: 6, under the second volume pump 42 pump pressures, liquid fat is by the material outlet of heat exchanger 43, the grease entrance 13 of corresponding pipeline and air film type reaction unit 1 enters in dish type atomization sparger 17.
Described Oleum Cocois is through refining impurity and the Oleum Cocois of hydrogenation after saturated removed, contained medium high carbon glycerin fatty acid ester is 95wt%～98wt%, in medium high carbon glycerin fatty acid ester, the glycerin fatty acid ester of 6～10 carbon accounts for 15wt%, 12, the glycerin fatty acid ester of 14 carbon accounts for 70wt%, and the glycerin fatty acid ester of 16,18 carbon accounts for 15wt%.
Described plam oil is also that contained medium high carbon glycerin fatty acid ester is 98.5wt%, is all the glycerin fatty acid ester of 16,18 carbon through refining impurity and the plam oil of hydrogenation after saturated removed.
3. under the second volume pump 42 pump pressures, liquid fat becomes vaporific drop ejection and enters in the upper cavity of tower main body 10 after dish type atomization sparger 17, under action of gravity, first fall on the filler of packing layer 21 of the first layer grid of the top, then carry out downward the flowing of general trend drops down onto on the filler of packing layer 21 of second layer grid along the surface of each filler again, under action of gravity, successively move downward again, and in flowing the filling surface of process form uniform liquid film.
4. 1. enter under the effect of the heat that the liquid methanol of tower main body 10 sends at spiral heater 18 and be vaporizated into methanol steam and pass through continuously from bottom to top packing layer 21 by step, react (so alcoholysis reaction is called steam film formula alcoholysis reaction or air film type alcoholysis reaction) thereby the catalyzed alcoholysis of medium high carbon fatty acid methyl ester and glycerine occurs under the effect at KOH with the grease in liquid film state on filler to generate this methanol steam in each packing layer 21.The time that grease stops at filler upper surface is can change by the loading height of adjusting packing layer 21 this residence time of 3～9min(, the present embodiment is 5min), because the complete reaction time of catalyzed alcoholysis reaction is about 3min, so the residence time of the present embodiment medium high carbon glycerin fatty acid ester in packing layer 21 is set to 5min, guarantees carrying out completely of alcoholysis reaction.The heat that the reaction heat that catalyzed alcoholysis reacts required is brought into by the medium high carbon glycerin fatty acid ester as raw material provides.
5. the medium high carbon fatty acid methyl ester being generated by step catalyzed alcoholysis reaction 4. and glycerine are under the effect of gravity, fall to the liquid storage portion 15 of the bottom of the tower main body 10 of air film type reaction unit 1, send in refining separating still and leave standstill by product pump 51 through by-pass valve control again, under action of gravity, sedimentation is separated into two-layer up and down, glycerine under, medium high carbon fatty acid methyl ester is upper.Separate glycerine from bottom, remaining medium high carbon fatty acid methyl ester is sent into crude product storage tank.
The reacted excessive methanol steam of catalyzed alcoholysis is motion from bottom to top in the tower main body 10 of air film type reaction unit 1, during through dish type atomization sparger 17, the space between the adjacent body of its coil pipe, pass, then rise to top and from the give vent to anger tower main body 10 of film type reaction device 1 of vapour outlet 14 Continuous Flow.
6. the medium high carbon fatty acid methyl ester 5. step being obtained is sent into and distillation tower, is carried out underpressure distillation from crude product storage tank, the residual voltage of controlling in distillation tower is that 10～20mm mercury column, temperature are 250 DEG C～280 DEG C, makes medium high carbon fatty acid methyl ester crude product become finished product by distilling.The methanol steam stream that step is flowed out continuously at the top of air film type reaction unit 1 in 5. enters in alcohol steam treatment system 6 by corresponding pipeline.Methanol steam first in the second heat exchanger 61 by the cooling liquid methanol that becomes of the refrigerated water as heat-eliminating medium (water of 7 DEG C～12 DEG C), this liquid methanol flows under the influence of gravity into liquid alcohol buffering withdrawing can 62 and pumps in operating tower reactor 1 through the first volume pump 33 and recycle.
(embodiment 2)
The rest part of the present embodiment is substantially the same manner as Example 1, difference is: the alcohol described in the present embodiment is ethanol instead of methyl alcohol, raw alcohol used is the dehydrated alcohol of purity >=99.5%, what in tower reactor 1, react generation with grease is glycerine and medium high carbon fatty-acid ethyl ester, the alcohol steam flowing out continuously at the top of air film type reaction unit 1 is alcohol vapour, and the alcohol for recycling in liquid alcohol buffering withdrawing can 68 is ethanol.
Claims (4)
1. a method for preparing medium-high carbon fatty acid ester by continuous alcoholysis, is characterized in that: have following steps:
1. continuously the excessive liquid alcohol that is dissolved with base metal catalysts in liquid alcohol storage tank (31) is pumped into the bottom the tower main body (10) of air film type reaction unit (1) by the first volume pump (33) from liquid alcohol entrance (12); Described liquid alcohol is methyl alcohol or ethanol; Described base metal catalysts is KOH or NaOH; The weight of base metal catalysts accounts for 0.1～0.5% of base metal catalysts and liquid alcohol gross weight;
2. carry out step 1. in, continuously the liquid fat in insulated tank (41) is pumped in operating heat exchanger (43) and made it to be heated to 120 DEG C～150 DEG C by the second volume pump (42) taking the mol ratio of grease and liquid alcohol as the ratio of 1: 5～1: 7, under the second volume pump (42) pump pressure, grease is entered in dish type atomization sparger (17) by the grease entrance (13) of the material outlet of heat exchanger (43), corresponding pipeline and air film type reaction unit (1); Described grease is medium high carbon glycerin fatty acid ester, and wherein the carbonatoms of the carbochain of medium high carbon fatty acid radical is 6 to 18;
3. under the second volume pump (42) pump pressure, liquid fat becomes vaporific drop ejection and enters in the upper cavity of tower main body (10) after dish type atomization sparger (17), under action of gravity, after falling on filler, the surface along filler is carried out downward the flowing of general trend and is successively dropped down onto on the filler of lower floor more then, and in flowing the filling surface of process form uniform liquid film;
4. 1. enter under the effect of the heat that the liquid alcohol of tower main body (10) sends at spiral heater (18) and be vaporizated into alcohol steam and pass through continuously from bottom to top packing layer (21) by step, react thereby the catalyzed alcoholysis of medium high carbon fatty acid ester and glycerine occurs under the effect at base metal catalysts with the grease in liquid film state on filler to generate this alcohol steam in each packing layer (21);
5. the medium high carbon fatty acid ester being generated by step catalyzed alcoholysis reaction 4. and glycerine are under the effect of gravity, fall to the liquid storage portion (15) of the bottom of the tower main body (10) of air film type reaction unit (1), passing through by-pass valve control is sent in refining separating still and is left standstill by product pump (51) again, under action of gravity, sedimentation is separated into two-layer up and down, glycerine under, medium high carbon fatty acid ester is upper; Separate glycerine from bottom, remaining medium high carbon fatty acid ester is sent into crude product storage tank; After catalyzed alcoholysis reaction, excessive alcohol steam is motion from bottom to top in the tower main body (10) of air film type reaction unit (1), during through dish type atomization sparger (17), the space between the adjacent body of its coil pipe, pass, then rise to top and from the give vent to anger tower main body (10) of film type reaction device (1) of vapour outlet (14) Continuous Flow.
2. the method for preparing medium-high carbon fatty acid ester by continuous alcoholysis according to claim 1, is characterized in that: also have following step:
6. the medium high carbon fatty acid ester crude product 5. step being obtained is refined: medium high carbon fatty acid ester crude product is sent into and in distillation tower, carried out underpressure distillation, the residual voltage of controlling in distillation tower is that 10～20mm mercury column, temperature are 250 DEG C～280 DEG C, makes medium high carbon fatty acid ester crude product become finished product by distilling; The alcohol vapour stream that step is flowed out continuously at the top of air film type reaction unit (1) in 5. enters by corresponding pipeline in alcohol steam treatment system (6), by refrigerated water as heat-eliminating medium by the cooling alcohol vapour stream liquid alcohol that becomes, this liquid alcohol can be recycled.
3. the method for preparing medium-high carbon fatty acid ester by continuous alcoholysis according to claim 1, is characterized in that: the base metal catalysts of step in is 1. KOH.
4. the method for preparing medium-high carbon fatty acid ester by continuous alcoholysis according to claim 1, is characterized in that: the grease of step in 2. and the mol ratio of liquid alcohol are 1: 6.
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| CN102512838A (en) * | 2011-12-30 | 2012-06-27 | 浙江工业大学 | Structured corrugated packing bed suitable for high liquid quantity |
| CN104479885A (en) * | 2014-11-28 | 2015-04-01 | 浙江赞宇科技股份有限公司 | Method and device for continuously producing triglyceride |
| CN107243299B (en) * | 2016-11-18 | 2018-09-07 | 湖南长科诚享石化科技有限公司 | A kind of reaction unit and a kind of reaction system and a kind of liquid-phase hydrogenatin reaction method |
| CN107858209A (en) * | 2017-12-12 | 2018-03-30 | 江西艾迪尔新能源有限公司 | A kind of method using vegetable oil as raw material continuous production fatty-acid ethyl ester |
| CN107987977A (en) * | 2017-12-12 | 2018-05-04 | 江西艾迪尔新能源有限公司 | A kind of production method of epoxidized soybean oil |
| CN112076700B (en) * | 2019-11-14 | 2023-06-23 | 海盐县精细化工有限公司 | Esterification kettle and application method thereof |
| CN114806722B (en) * | 2022-05-06 | 2024-04-05 | 宁波杰森绿色能源科技有限公司 | System and method for continuously producing fatty acid methyl ester |
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| CN101195572A (en) * | 2006-12-08 | 2008-06-11 | 四川古杉油脂化学有限公司 | Method for synthesizing fatty acid methyl ester |
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| CN101747182A (en) * | 2008-12-01 | 2010-06-23 | 浙江东江能源科技有限公司 | Low acid value esterification novel process |
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| PT1034160E (en) * | 1997-11-24 | 2002-10-31 | Energea Umwelttechnologie Gmbh | METHOD FOR THE PRODUCTION OF FATTY ACID METHYL ESTER AND EQUIPMENT FOR PERFORMING THE SAME |
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| CN101195572A (en) * | 2006-12-08 | 2008-06-11 | 四川古杉油脂化学有限公司 | Method for synthesizing fatty acid methyl ester |
| CN101550082A (en) * | 2008-04-02 | 2009-10-07 | 拜耳技术工程（上海）有限公司 | Method and device for continuously producing carboxylic ether |
| CN101747182A (en) * | 2008-12-01 | 2010-06-23 | 浙江东江能源科技有限公司 | Low acid value esterification novel process |
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