KR102307469B1 - Biodiesel production system including high acid oil pretreatment using biodiesel by-products - Google Patents

Abstract

The present invention relates to a system for producing biodiesel after reducing the free fatty acid content of oil (hereinafter, high acid value oil) containing a large amount (2.6 to 60%) of free fatty acids (FAA, Free Fatty Acid). A high acid value oil pretreatment reaction unit including a high acid value reaction tank for producing low acid value oil with reduced free fatty acid content (less than 2.5%) by mixing glycerin with high acid value oil and low acid value oil, methanol and catalyst discharged from the high acid value oil pretreatment reaction unit A low acid value reactor for injecting and mixing, a precipitation tank for precipitating and discharging glycerin, a methanol recovery tank for recovering methanol, a washing tank for washing after methanol recovery, a drying tank for removing water after washing, and a bio-water from which water is removed from the drying tank A biodiesel production system comprising a biodiesel synthesis reaction unit including a biodiesel storage tank for storing diesel, and a high acid value oil pretreatment process using biodiesel by-products used by sending glycerin separated and discharged from the settling tank to a high acid value oil pretreatment reaction unit is about
The biodiesel production system including the high acid value oil pretreatment process using the biodiesel by-product according to the present invention uses glycerin to produce a high acid value oil with a high free fatty acid content into a low acid value oil with a low free fatty acid content to produce biodiesel. It can be applied to a large amount of high acid value oil at a relatively low temperature of 90 ~ 105 ° C. by reducing the overtime and performing the mixing reaction of high acid value oil and glycerin using a static mixer and a cavitation reactor, and when producing biodiesel of low acid value oil By using the generated glycerin, the free fatty acid content of the high acid value oil is lowered and the composition of purifying the glycerin is added to produce biodiesel with a high yield.

Description

Biodiesel production system including high acid oil pretreatment using biodiesel by-products

The present invention relates to a system for producing biodiesel after reducing the free fatty acid content of fats and oils (hereinafter, high acid value oil) containing a large amount (2.6 to 60%) of free fatty acids (FAA, Free Fatty Acid). A high acid value oil pretreatment reaction unit including a high acid value reaction tank for producing low acid value oil with reduced free fatty acid content (less than 2.5%) by mixing glycerin with high acid value oil and low acid value oil, methanol and catalyst discharged from the high acid value oil pretreatment reaction unit A low acid value reaction tank for injecting and mixing, a precipitation tank for precipitating and discharging glycerin, a methanol recovery tank for recovering methanol, a washing tank for washing after methanol recovery, a drying tank for removing water after washing, and a bio-water from which water is removed from the drying tank A biodiesel production system comprising a biodiesel synthesis reaction unit including a biodiesel storage tank for storing diesel, and a high acid value oil pretreatment process using biodiesel by-products used by sending glycerin separated and discharged from the settling tank to a high acid value oil pretreatment reaction unit is about

Biodiesel is a fatty acid alkyl ester manufactured by reacting animal and vegetable oils and fats with alcohol, and is highly anticipated as an alternative fuel to petroleum diesel. It has the advantage of low carbon dioxide emission. In general, biodiesel is produced by a transesterification method that reacts with low-priced methanol among alcohols under an acid/alkali catalyst. Base catalysts, acid catalysts, and enzyme catalysts are used depending on characteristics such as acid value of raw materials. synthesized in a variety of ways. For biodiesel synthesis by transesterification method, oils and fats with a free fatty acid content of 2.5% or less are used, and a base catalyst has a faster reaction time than an acid catalyst and is mainly used because of its high productivity. A catalyst for separating the catalyst after the production of biodiesel A neutralization process, a washing process to remove salts generated in this process, and a drying process to remove water are involved.

In the production of biodiesel using general triglycerides (TG, triglyceride), the reaction chemical formula is as follows: methanol and catalyst are mixed to form diglyceride, diglyceride is reacted with methanol and catalyst to form monoglyceride, and then methanol and catalyst are reacted to form a monoglyceride. Biodiesel is produced by generating glycerin.

On the other hand, since more than 70% of the cost of biodiesel production is made by the raw material price, it is possible to lower the production cost by using raw materials such as waste cooking oil and food waste oil with low raw material prices, but the above raw materials are free fatty acids (FAA, It is a high acid value oil with a high content of Free Fatty Acid), and the process of producing biodiesel and lowering the free fatty acid content using an acid catalyst should be carried out. Specifically, the conventional high acid value oil containing a lot of free fatty acids consists of triglycerides (TG, triglyceride) and free fatty acids. First, in order to reduce the content of free fatty acids, a biodiesel reaction using methanol and an acid catalyst is used to reduce the content of free fatty acids. Reduce the content of free fatty acids. At this time, the water produced is removed and the methanol is removed by evaporation under reduced pressure to produce a low-acid oil with a free fatty acid content of 2.5% or less, and then use the low-acid oil to produce biodiesel using methanol and a base catalyst. It is a situation in which complex processes such as procedures are being carried out. Due to this, the process is complicated, and since it has a problem that it takes a lot of time and cost for production, a very high content (about 97 to 99%) of triglycerides or free fatty acids is used. However, the raw materials generated in the market have a problem that the raw materials of the high acid value oil containing a large amount of free fatty acids in triglycerides make up most of them.

Recently, as prior technologies for producing biodiesel using high acid value oil containing a large amount of free fatty acids, Korea Patent No. 10-2043442 (November 11, 2019) discloses a method for refining or purifying oils and fats containing animal and vegetable oils containing a large amount of free fatty acids. High-quality low-acid biodiesel by inducing an accurate reaction by preventing glycerin from being lost before completion of the reaction through a process of condensing and re-injecting glycerin that is vaporized with moisture during the reaction process with non-catalyst high-vacuum heating reaction with unrefined glycerin A method for producing low-acid glycerides for biodiesel raw materials without using a catalyst for fats and oils containing a large amount of fatty acids and free fatty acids for generating glycerides for use is provided, and Korean Patent Application Laid-Open No. 10-2008-0015758 (February 20, 2008) .) is a reaction of a free fatty acid feedstock with glycerin to convert it to glyceride, and the amount of glycerin is added in a stoichiometric ratio of glycerin to free fatty acid of about 35 to 40%, and at 150 to 250° C. for 30 to 500 minutes. It provides for the production of biodiesel and glycerin from higher free fatty acid feedstocks carried out during the period but in the absence of a catalyst.

Looking at the prior art, when adjusting the high acid value oil to the low acid value oil, glycerin is used to achieve a simpler process than the prior art, and the glycerin used is used using glycerin generated during biodiesel production. However, glycerin used in the prior art forms a complicated process even if unrefined or purified glycerin is used, and low acid value oil production by adding glycerin is carried out at 100 to 250° C. under high pressure or vacuum. It has a problem in that it is difficult to apply it when a large amount of high-acid oil is used.

Korean Patent Registration No. 10-2043442 (2019.11.11.) Korea Patent Publication No. 10-2008-0015758 (2008.02.20.)

The technical task to be achieved by the present invention is to simplify the process of lowering the free fatty acid content by adding methanol and an acid catalyst to the high acid value oil having a high free fatty acid content of the prior art using glycerin, but the glycerin mixing reaction process is performed by cavitation of the present invention An object of the present invention is to provide a biodiesel production system including a high acid value oil pretreatment process using biodiesel by-products that can be carried out in large quantities at a low temperature using a reactor.

In order to solve the above problems and achieve the object, the biodiesel production system including the high acid value oil pretreatment process using the biodiesel by-product according to an embodiment of the present invention has a free fatty acid content of 2.6 to 60% by weight. A high acid value oil pretreatment reaction unit 100 including a high acid value reactor 120 for producing a low acid value oil in which the free fatty acid content is reduced to 1 to 2.5% by mixing glycerin with the high acid value oil contained therein; And the low acid value oil discharged from the high acid value oil pretreatment reaction unit 100, the low acid value reactor 210, which injects and mixes methanol and a catalyst, the mixture mixed in the low acid value reactor 210 is injected, and glycerin is precipitated and discharged separately a precipitation tank 220, a methanol recovery tank 230 for recovering methanol by injecting a mixture from which glycerin is separated in the precipitation tank 220, a washing tank 240 for washing after methanol recovery, and washing to remove impurities and then water and a biodiesel synthesis reaction unit 200 including a drying tank 250 and a biodiesel storage tank 260 for storing biodiesel from which water has been removed from the drying tank 250; and the settling tank 220 The glycerin separated and discharged from the glycerin is injected into the glycerin storage tank 222 and then introduced into the glycerin discharge tank 224 to remove salt and sent to the high acid value oil pretreatment reaction unit 100 .

In the biodiesel synthesis reaction unit 200, the glycerin storage tank 222 adds and mixes a strong acid of pH 1 to 3 to the injected glycerin, adjusts the pH of the glycerin to pH 5 to 7, and discharges the glycerin discharge tank 224. The salt is then precipitated and removed.

The high acid value oil pretreatment reaction unit 100 introduces the high acid value oil of the high acid value reactor 120 and the glycerin from which the salt has been removed from the glycerin discharge tank 224 of the biodiesel synthesis reaction unit 200 into the static mixer 110. After tea mixing, the mixed mixture is injected into the cavitation reactor 300 for a mixed reaction, and then re-injected downward from the upper surface of the high acid value reactor 120 .

The high acid value oil pretreatment reaction unit 100 circulates the reintroduced mixture to the static mixer 110, the cavitation reactor 300 and the high acid value reactor 120 a plurality of times to produce a low acid value oil, and in the process of circulating water and The impurities are discharged and removed from the high acid value reactor 120 using the vacuum/condensing device 130, and the prepared low acid value oil is discharged.

The high acid value reactor 120 is installed with a plurality of helical coil nozzles (not shown) attached to the inner upper surface, and the mixture discharged from the cavitation reactor 300 is injected while spraying into the high acid value reactor 120 .

The cavitation reactor 300 has a driving motor unit 310 and a rotating shaft of the driving motor unit 310 inserted therein, and a cooling unit including a cooling water inlet 322 and a cooling water outlet 324 for introducing and discharging cooling water. (320), the raw material inlet 332 for mixing the mixture discharged from the static mixer 110 and the raw material outlet 334 for discharging, the rotating body 336 fixedly connected to the rotating shaft, and the rotating body 336 and a mixing reaction unit 330 including a fixture 338 positioned to face each other so that a predetermined interspace is formed, and the mixture is introduced from the raw material inlet 332 into the space between the mixing reaction unit 330 and then mixed It reacts and comprises a clearance adjustment unit 340 for adjusting the interval between the fixed body 338 to flow.

The fixed body 338 and the rotating body 336 are disk-shaped, and the opposite side is formed to form a flat surface or a curved surface to be rotatable, but is formed to mesh, and the mixture reacts with the rotation of the rotating body While being moved outward by centrifugal force, it is discharged to the raw material outlet 334 .

The driving motor unit 310 is installed in connection with the rotating body 336 through the rotating shaft passing through the cooling unit 320, and is installed by being directly connected to the rotating body 336 or the driving motor unit 310 is installed on one side. Provided is a biodiesel production system including a high acid value oil pretreatment process using biodiesel by-products that are installed and connected to the belt 350 to be driven.

As described above, the biodiesel production system including the high acid value oil pretreatment process using the biodiesel by-product according to the present invention has the following effects.

(1) The present invention reduces production cost and time by producing biodiesel by manufacturing high acid value oil with high free fatty acid content into low acid value oil with low free fatty acid content using glycerin.

(2) The present invention can be applied to a large amount of high acid value oil at a relatively low temperature of 90 to 105° C. by performing the mixing reaction of high acid value oil and glycerin using a static mixer and a cavitation reactor.

(3) The present invention can produce high yield of biodiesel by using glycerin generated during biodiesel production of low acid value oil to lower the free fatty acid content of high acid value oil and purifying the glycerin.

1 is a block diagram of a biodiesel production system including a high acid value oil pretreatment process using biodiesel by-products according to a preferred embodiment of the present invention.
2 is a block diagram showing a high acid value oil pretreatment reaction unit according to a preferred embodiment of the present invention.
3 is a block diagram showing a sedimentation tank, a glycerin storage tank, and a glycerin discharge tank of the biodiesel synthesis reaction unit according to a preferred embodiment of the present invention.
4 is a front view of a cavitation reactor according to a preferred embodiment of the present invention.
5 is a cross-sectional view of a cavitation reactor according to a preferred embodiment of the present invention.
6 is an exemplary configuration diagram of a cavitation reactor according to an embodiment of the present invention.

The title of the present invention is "biodiesel production system including a high acid value oil pretreatment process using biodiesel by-products" and describes specific details so that those skilled in the art can easily understand it, and omits a separate description that can be sufficiently inferred, if necessary Examples and drawings are described. In addition, the terms defined in the present specification and claims are not limited to interpretation, may vary according to the intention or custom of the operator, etc., and should be interpreted as meanings and concepts consistent with the technical spirit of the present invention.

In one aspect of the present invention,

1 is a block diagram of a biodiesel production system including a high acid value oil pretreatment process using biodiesel by-products according to a preferred embodiment of the present invention. Referring to FIG. 1 , the biodiesel production system of the present invention will be described below.

In the biodiesel production system including a pretreatment process for reducing the free fatty acid content contained in high acid value oil,

The biodiesel production system is

High acid value oil pretreatment including a high acid value reactor 120 that mixes glycerin with high acid value oil containing 2.6 to 60% of free fatty acids by weight to produce low acid value oil in which the free fatty acid content is reduced to 1 to 2.5% and then discharges reaction unit 100; and

The low acid value oil discharged from the high acid value oil pretreatment reaction unit 100, the low acid value reactor 200 in which methanol and catalyst are injected and mixed, and the mixture mixed in the low acid value reactor 200 is injected, and glycerin is precipitated and discharged separately A precipitation tank 220, a methanol recovery tank 230 for recovering methanol by injecting a mixture from which glycerin is separated in the precipitation tank 220, a washing tank 240 for washing after methanol recovery, and washing to remove impurities and then water and a biodiesel synthesis reaction unit 200 including a drying tank 250 and a biodiesel storage tank 260 for storing biodiesel from which water has been removed from the drying tank 250; The separated and discharged glycerin is injected into the glycerin storage tank 222 and then introduced into the glycerin discharge tank 224 to remove salt and sent to the high acid value oil pretreatment reaction unit 100 .

The chemical reaction formula of free fatty acid (FAA, Free Fatty Acid) and glycerin is shown below.

In the high acid value oil pretreatment reaction unit 100, the mixing amount of glycerin is added as 1/3 to 1/6 of free fatty acid (FAA, Free Fatty Acid) in a weight ratio. The production yield is lowered.

The low acid value oil is an oil whose free fatty acid content is adjusted to 2.5% or less, and biodiesel production is carried out by inputting a basic catalyst and methanol, a general transesterification method, and the glycerin generated at this time is used as glycerin input to the high acid value reactor. There is no need for glycerin wastewater treatment.

3 is a block diagram showing a sedimentation tank, a glycerin storage tank, and a glycerin discharge tank of the biodiesel synthesis reaction unit according to a preferred embodiment of the present invention. Referring to FIG. 3, the process of treating glycerin in the biodiesel synthesis reaction unit of the present invention proceed below.

In the biodiesel synthesis reaction unit 200, the glycerin storage tank 222 adds and mixes a strong acid of pH 1 to 3 to the injected glycerin, adjusts the pH of the glycerin to pH 5 to 7, and discharges the glycerin discharge tank 224. The salt is then precipitated and removed.

The glycerin precipitated in the precipitation tank 220 is discharged to the glycerin storage tank 222, and the discharged glycerin is maintained at pH 12 by the base catalyst injected in the low acid value reaction tank 210, so a strong acid (sulfuric acid, etc.) of pH 1 to 3 is It is preferable to adjust the pH to 5 to 7 by input, and at this time, the pH is adjusted while circulating while adding a strong acid.

After pH adjustment, salt is removed by precipitation in the glycerin discharge tank 224 , and then glycerin is sent to the high acid value oil pretreatment reaction unit 100 .

2 is a block diagram showing a high acid value oil pretreatment reaction unit according to a preferred embodiment of the present invention, and the high acid value oil pretreatment reaction unit of the present invention will be described below with reference to FIG. 2 .

The high acid value oil pretreatment reaction unit 100 introduces the high acid value oil of the high acid value reactor 120 and the glycerin from which the salt has been removed from the glycerin discharge tank 224 of the biodiesel synthesis reaction unit 200 into the static mixer 110. After tea mixing, the mixed mixture is injected into the cavitation reactor 300 for a mixed reaction, and then re-injected downward from the upper surface of the high acid value reactor 120 .

The static mixer 110 (static mixer = line mixer) is an element element, that is, an element in which frames such as spirals having different directions are attached to each other are installed inside the line, and as the mixture passes through the line, the mixture is stirred. it will be carried out

The cavitation reactor 300 injects the first mixed mixture in the static mixer 110, and the reaction is mixed in a state of 90 to 105°C.

The high acid value oil pretreatment reaction unit 100 circulates the reintroduced mixture to the static mixer 110, the cavitation reactor 300 and the high acid value reactor 120 a plurality of times to produce a low acid value oil, and in the process of circulating water and The impurities are discharged and removed from the high acid value reactor 120 using the vacuum/condensing device 130, and the prepared low acid value oil is discharged.

The vacuum/condensing device 130 pressurizes the inside of the high acid value reactor 120 in a vacuum state, but at this time, the high acid value reaction tank internal temperature is maintained at 90 ~ 105 ° C. to remove water and foreign substances.

The high acid value reactor 210 is installed with a plurality of helical coil nozzles (not shown) attached to the inner upper surface, and the mixture discharged from the cavitation reactor 300 is injected while spraying into the high acid value reactor 120 .

The mixture containing a lot of glycerin, which is precipitated from the mixture evenly jetted into the high acid value reactor 120 by the helical nozzle in the high acid value reactor 120, is recycled through the outlet of the bottom surface of the high acid value reactor 120, and the bottom surface Before discharging through the outlet, the mixture adjusted to the low acid value oil is sent to the biodiesel synthesis reaction unit 200 by having an outlet on one side of the upper side.

4 is a front view of a cavitation reactor according to a preferred embodiment of the present invention, FIG. 5 is a cross-sectional view of a cavitation reactor according to a preferred embodiment of the present invention, and FIG. 6 is a cavitation reactor according to a preferred embodiment of the present invention. The cavitation reactor of the present invention will be described below with reference to FIGS. 4 to 6 as an exemplary configuration of the .

The cavitation reactor 300 has a driving motor unit 310 and a rotating shaft of the driving motor unit 310 inserted therein, and a cooling unit including a cooling water inlet 322 and a cooling water outlet 324 for introducing and discharging cooling water. (320), the raw material inlet 332 for mixing the mixture discharged from the static mixer 110 and the raw material outlet 334 for discharging, the rotating body 336 fixedly connected to the rotating shaft, and the rotating body 336 and a mixing reaction unit 330 including a fixture 338 positioned to face each other so that a predetermined interspace is formed, and the mixture is introduced from the raw material inlet 332 into the space between the mixing reaction unit 330 and then mixed It reacts and comprises a clearance adjustment unit 340 for adjusting the interval between the fixed body 338 to flow.

The mixture is introduced between the rotating body 336 and the fixed body 338 of the mixing reaction unit 330, and the rotating body 336 is rotated at a high speed by the driving motor 310 to perform a mixing reaction to generate cavitation. In the process, micro jets are generated so that the mixing reaction can proceed quickly. On the other hand, heat generated by the rotation of the rotating body 336 passes through a surface positioned to be wrapped around the outer surface of the rotating body 336 by injecting cooling water through the cooling water inlet 322, and discharged through the cooling outlet 324. to prevent the temperature rise of the rotating body 336, and the mixture after the mixing reaction is put into the high acid value reactor 120 to remove water and foreign substances at a temperature of 90 to 105° C. and a reduced pressure state, but the mixed reaction through the cavitation reactor Since this is carried out by adding the mixture, water and foreign matter can be removed smoothly even at the above temperature.

The fixed body 338 and the rotating body 336 have a flat surface or a curved surface to be rotatable in a disk shape so that a surface formed to be engaged or a protruding surface and a recessed surface are facing each other. It is made of the formed surface, and as the mixture reacts with the rotation of the rotating body 336 , it is moved outward by centrifugal force and discharged to the raw material outlet 334 .

The driving motor unit 310 is installed in connection with the rotating body 336 through the rotating shaft passing through the cooling unit 320, and is installed by being directly connected to the rotating body 336 or the driving motor unit 310 is installed on one side. It can be installed and connected to the belt 350 to be driven.

In addition, the cavitation reactor 300 may be used even in the production of low acid value oil, in which case the cavitation reactor 300 injects high acid value oil into the raw material inlet 332, and additionally methanol and a catalyst are added. In addition, it can be carried out.

In a further aspect,

Separation of biodiesel and glycerin in the precipitation tank 220 separates the precipitated glycerin after precipitation and discharges it to the glycerin storage tank 222. The downside is that it exists. Therefore, a circular or rectangular plate in the form of a mesh is placed between the anodes, and the anode and the plate are put into the settling tank 220 to pass electricity. At this time, when electricity passes, glycerin is attached to the net, and when the attached glycerin is combined and produced at a constant weight, it is precipitated downward of the settling tank 220 to separate glycerin. can

In the case of a high acid value oil having a content of 61 to 90% of the free fatty acid, a pretreatment process of lowering the acid value by using a rapase enzyme as a catalyst and adding methanol and lowering the acid value may be added. At this time, the acid value can be lowered by mixing the high acid value oil and the rapase enzyme in a weight ratio of 1:0.05, and mixing methanol by dividing the mixture several times.

As described above, the biodiesel production system including the high acid value oil pretreatment process using the biodiesel by-product according to the present invention uses glycerin to produce a high acid value oil with a high free fatty acid content into a low acid value oil with a low free fatty acid content to produce biodiesel. It reduces production cost and time by producing By using glycerin generated during biodiesel production, the free fatty acid content of high acid value oil is lowered, and the composition of purifying the glycerin is added to produce biodiesel with a high yield.

As described above, although the present invention has been described with reference to limited examples and drawings, the present invention is not limited thereto, and the technology to which the present invention belongs is within the scope of equivalents of the technical spirit of the invention and the claims to be described below. Of course, various modifications and variations are possible.

100: high acid value oil pretreatment reaction unit 300: cavitation reactor
110: static mixer 310: drive motor unit
120: high acid value reactor 320: cooling unit
130: vacuum condensing device 322: cooling water inlet
200: biodiesel synthesis reaction unit 324: cooling water outlet
210: low acid value reactor 330: mixed reaction unit
220: settling tank 332: raw material inlet
222: glycerin storage tank 334: raw material outlet
224: glycerin discharge tank 336: rotating body
230: methylol recovery tank 338: fixed body
240: washing tank 340: clearance adjustment unit
250: drying tank 350: belt
260: biodiesel storage tank

Claims (8)

In the biodiesel production system including a pretreatment process for reducing the free fatty acid content contained in high acid value oil,
The biodiesel production system is
A high acid value reactor that produces low acid value oil with a free fatty acid content reduced to 1 to 2.5% by mixing glycerin with a high acid value oil containing 2.6 to 60% of free fatty acids by weight at a temperature of 90 to 105 ° C. High acid value oil pretreatment reaction unit; and
A low acid value reactor in which the low acid value oil discharged from the high acid value oil pretreatment reaction unit, methanol, and a catalyst are injected and mixed, the mixture mixed in the low acid value reactor is injected, and glycerin is precipitated and discharged separately. In the settling tank, glycerin is separated A methanol recovery tank for recovering methanol by injecting the mixture, a washing tank for washing after methanol recovery, a drying tank to remove water after washing to remove impurities, and a biodiesel storage tank for storing biodiesel from which water has been removed from the drying tank It consists of a biodiesel synthesis reaction unit;
After the glycerin separated and discharged from the settling tank is injected into the glycerin storage tank, the salt is removed by putting it into the glycerin discharge tank, and it is sent to the high acid value oil pretreatment reaction unit,
In the biodiesel synthesis reaction part, the glycerin storage tank adds a strong acid of pH 1 to 3 to the injected glycerin, mixes it, adjusts the pH of glycerin to pH 5-7, discharges the glycerin discharge tank, and precipitates salt to remove it A biodiesel production system comprising a high acid value oil pretreatment process using biodiesel by-products. delete According to claim 1,
The high acid value oil pretreatment reaction unit first mixes the high acid value oil of the high acid value reactor and the glycerin from which the salt has been removed from the glycerin discharge tank of the biodiesel synthesis reaction unit into a static mixer, and the mixed mixture is injected into the cavitation reactor for mixing reaction. A biodiesel production system comprising a high acid value oil pretreatment process using biodiesel by-products, characterized in that re-injection from the upper surface of the high acid value reactor downward. 4. The method of claim 3,
The high acid value oil pretreatment reaction unit circulates the reintroduced mixture to a static mixer, a cavitation reactor and a high acid value reactor a plurality of times to produce a low acid value oil, and in the process of circulation, water and impurities are discharged from the high acid value reactor using a vacuum/condensing device. A biodiesel production system comprising a high acid value oil pretreatment process using biodiesel by-products, characterized in that removing and discharging the manufactured low acid value oil. 4. The method of claim 3,
The high acid value reactor includes a high acid value oil pretreatment process using biodiesel by-products, characterized in that the mixture discharged from the cavitation reactor is injected into the high acid value reactor by attaching a plurality of helical nozzles to the inner upper surface of the reactor production system. 4. The method of claim 3,
In the cavitation reactor, a driving motor unit, a rotating shaft of the driving motor unit are inserted, a cooling unit including a cooling water inlet and a cooling water outlet for introducing and discharging cooling water, and a raw material inlet for introducing the mixture discharged from the static mixer after mixing A mixture is introduced from the raw material inlet into the space between the raw material discharge port for discharging, the rotating body fixedly connected to the rotating shaft, and a fixed body positioned to face the rotating body to form a predetermined space between the rotating body and the mixing reaction unit A biodiesel production system comprising a high acid value oil pretreatment process using biodiesel by-products, characterized in that it comprises a gap adjusting unit for controlling the space between the two parts by mixing and reacting the fixed body by flowing the fixed body. 7. The method of claim 6,
The fixed body and the rotating body are disk-shaped, and the opposite side is formed to form a flat surface or to form a curve to be rotatable, but to be formed to mesh, and the mixture reacts with the rotation of the rotating body to outward by centrifugal force A biodiesel production system comprising a high acid value oil pretreatment process using biodiesel by-products, characterized in that they are moved and discharged to a raw material outlet. 7. The method of claim 6,
The driving motor unit is a biodiesel by-product, characterized in that the rotating shaft passes through the cooling unit and is connected to the rotating body and rotates, and is installed directly connected to the rotating body or the driving motor unit is installed on one side and connected with a belt to be driven A biodiesel production system including a high acid value oil pretreatment process.

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