CN101343550A

CN101343550A - Production process of biological diesel oil

Info

Publication number: CN101343550A
Application number: CNA2007100153740A
Authority: CN
Inventors: 张国滨
Original assignee: Individual
Current assignee: Individual
Priority date: 2007-07-10
Filing date: 2007-07-10
Publication date: 2009-01-14

Abstract

The invention provides a biodiesel production method, which adopts the steps: firstly, animal and vegetable fats and oils are put into a reactor to be heated, and are settled after citric acid and salt water being added and stirred, thus pre-esterified animal and vegetable fats and oils are obtained; secondly, concentrated sulfuric acid and methyl alcohol are added into the pre-esterified animal and vegetable fats and oils, a circumfluence reaction is performed after being stirred and reacted, to obtain pre-esterified materials; thirdly, the esterified materials are put into a fractionating tower to be fractionated, and fatty acid methyl esters are fractionated out; fourthly, fractionated fatty acid methyl is decolored, separated and filtered to obtain biodiesel. The biodiesel produced with the method has the advantages that the viscosity of the biodiesel is low, the color is light, the freezing point is low and can be decreased by 0.5 DEG C 1 DEG C, the cetane value is high, the carbochain is reduced to C18 to C20, the free acid content is less than 0.5 percent, and the yield of the fatty acid methyl ester reaches more than 90 percent. In addition, the material with good fluidity is not required to be selected.

Description

A kind of production method of biofuel

Technical field

The invention provides a kind of production method of biofuel.

Background technology

At present, utilize soya-bean oil, Oleum Gossypii semen, lard, sewer oil, frying wet goods animal-plant oil production method of bio-diesel oil to be, animal-plant oil and methyl alcohol, catalyzer etc. are put into reactor carry out esterification, generate fatty acid methyl ester (being biofuel), then the raw glycerine of reactor bottom is emitted, the fatty acid methyl ester on reactor top is emitted, utilize condenser to isolate methyl alcohol excessive in the reaction.Owing to adopt 40-60 ℃ of technology of low temperature, be difficult at low temperatures raw glycerine, colloid, bituminous matter etc. are separated from fatty acid methyl ester, the purity of fatty acid methyl ester is low.Reaction time of esterification is also longer at low temperatures, and the partial fatty acid methyl esters can produce floatingization or reaction of degeneration, produces saponifiedly in a large number, has reduced the yield of fatty acid methyl ester.The biofuel viscosity of utilizing this method to produce is big, color and luster is dark, zero pour is high, after mineral diesel is mixed, could use under higher temperature, and then can't use northerly winter, can only be used as oil fuel.And behind life-time service on the automobile, can produce coking, stop up oil nozzle.

Summary of the invention

Technical problem to be solved by this invention is to provide a kind of production method of biofuel, to improve the quality of the biofuel of being produced.

The present invention is achieved in that a kind of production method of biofuel, and the step that described method adopts is,

A, animal-plant oil is sent in the reactor, when animal-plant oil is heated to 32-37 ℃, the citric acid of animal-plant oil weight 0.2-0.4% is put in the animal-plant oil, then under 48-52 ℃ of temperature, stirred 15-20 minute, again with the industrial table salt of animal-plant oil weight 0.2-0.4%, the composite salt solution of water of animal-plant oil weight 8-12% joins in the animal-plant oil, in 18-22 minute, stir, stop heating when heating to 88-92 ℃, sedimentation 3.5-4.5 hour, remove the water that is deposited in reactor bottom, colloid and part raw glycerine, the animal-plant oil after the pre-esterification treatment;

B, the vitriol oil joined in the methyl alcohol stir, the vitriol oil, the consumption of methyl alcohol is respectively the 0.5-2% of the animal-plant oil weight after the above-mentioned pre-esterification treatment and the 18-22% of the animal-plant oil weight after the above-mentioned pre-esterification treatment, stir after 18-22 minute, it is joined in the animal-plant oil after the above-mentioned pre-esterification treatment in the reactor, stirring reaction 18-22 minute, heat then to 72-90 ℃ and open reactor and reflux between valve, carried out back flow reaction 2.8-3.2 hour, stop then heating, when the material temperature in the reactor is reduced to 35-40 ℃, weak base with the animal-plant oil weight 0.1-0.3% after the above-mentioned pre-esterification treatment, the mixture that the methanol mixed reaction of animal-plant oil weight 18-22% after the above-mentioned pre-esterification treatment formed in 18-22 minute, join in the reactor, heat to 72-130 ℃ and back flow reaction 3.8-4.2 hour once more, in twice back flow reaction process, the pressure in the reactor is 0.1-0.5Mpa, the material after the esterification;

C, material after the above-mentioned esterification is sent into the bottom to be had heating unit, middle part to have adsorption stuffing device, top to have in the separation column of condensing works to carry out fractionation, with the cut point that contains in the material be lower than 70 ℃ methyl alcohol, the fatty acid methyl ester fractionation that cut point is 70-360 ℃ is come out;

D, the fatty acid methyl ester that above-mentioned fractionation is come out decolours, separation, filtration treatment, makes biofuel.

The biofuel viscosity that adopts aforesaid method to produce is low, lighter color, zero pour low (can reduce 0.5-1 ℃), the cetane value height, carbochain is reduced to C18-C20, free acid content is lower than 0.5%, viscosity reduces to 6 by 17.2 of original technology, colourity reduces to 3 by 4 of original technology, and the yield of fatty acid methyl ester reaches more than 90%.After testing, every index of the biofuel of the present invention's method production meets the examination criteria of German biofuel fully.And in this production method, as long as tankage, acidifying wet goods that condensation point is lower than behind 30 ℃ the animal-plant oil, waste oil, animal-plant oil refining can needn't be selected the raw material of good fluidity as raw material.

Description of drawings

Fig. 1 is the synoptic diagram of reflux structure used among the present invention.

Fig. 2 is the synoptic diagram of separation column structure used among the present invention.

Embodiment

Below in conjunction with further specifying the present invention.

Described weak base is a kind of in yellow soda ash, the sodium phosphate.

As shown in Figure 1, backflow body 1-5 is arranged on reflux, return line is external cooling water circulation body 1-6, return line intracoelomic cavity bottom goes out to manage that 1-1 communicates, top is equipped with another butterfly valve 1-8 with reactor through butterfly valve 1-3, cooling water intake 1-4, the cooling water outlet 1-10 that install the upper and lower part in the cooling water circulation pipe outside respectively with backflow body, cooling water circulation body between cavity communicate.

The upper and lower end of backflow body is curved, and pressure safety valve interface 1-9 and thermometer interface 1-7 are arranged in the upper end of backflow body.Going out to manage at reactor has visor 1-11 on the 1-1, its side also is communicated with venting port 1-2.

Open the valve between reactor and the reflux, when carrying out back flow reaction, the materials such as fatty acid methyl ester that generate in the reactor, enter the return line intracoelomic cavity, by mobile water coolant heat exchange cooling in the cavity between backflow body, the cooling water circulation body, cooling forms circulation after transfer lime, reactor return pipe are got back in the reactor.

As shown in Figure 2, tower body shell 17 is arranged on separation column, in the tower body shell, there are steam heating tube 2, filler body 14, bottom that another filler body 13, the shell and tube cooler 9 of liquid distributor 6 are arranged from top to bottom successively, the tower body upper end has oil gas vent 10, bottom to have oil and gas import 16, lower end that sewage draining exit 1 is arranged, steam heating tube is connected with steam inlet 18, the vapour outlet 3 in the tower body outside, and shell and tube cooler is connected with entrance of cooling water 11, the cooling water outlet 8 in the tower body outside.

Filler body 14 be positioned at support refractory slab 15 above.The fillers such as filter sand excessively that absorption, filteration have been arranged in each filler body.Thermometer socket 4, feeding port 5, side line outlet 7 can also be arranged in the bottom of tower body shell, and feeding port is used to change filler.

During use, this separation column can vertically install and fix by the outer support 12 of tower body.

On this separation column, heating unit is made of steam heating tube 2 grades.The adsorption stuffing device is made of filler body 14, another filler body 13 etc.Formations such as condensing works shell and tube cooler.

During fractionation, the material after the esterification enters tower body bottom, be heated by steam the steam heating in the pipe after, upwards flow, after the absorption of two filler bodies, filtering, again by the cooling water temperature in the shell and tube cooler, and then the oil gas vent on tower body enters the condenser of establishing in addition.According to the difference of the material cut point in the material after the esterification, fatty acid methyl ester, methyl alcohol are separated.

Reactor can adopt reactor.Be deposited in water, colloid and the part raw glycerine of reactor bottom in the reaction process, can discharge by the sewage draining exit of reactor lower end and remove.

It is 98% the vitriol oil that the vitriol oil can adopt purity.

In the d step, decolouring can utilize atlapulgite or gac etc. to carry out.Can utilize slurry tank during separation, separate by the unclassified stores that sedimentation is different with proportion with fatty acid methyl ester.Filtration can utilize filter to finish.

Claims

1, a kind of production method of biofuel is characterized in that, the step that described method adopts is,

2, the production method of biofuel as claimed in claim 1 is characterized in that, described weak base is a kind of in yellow soda ash, the sodium phosphate.