KR102122047B1 - Method for manufacturing biofuel using a vacuum heating reactor - Google Patents

Abstract

The present invention relates to a method for manufacturing biodiesel using a vacuum heating reactor, which produces biodiesel, which comprises monoglyceride and diglyceride and has an acid value of 25 or less, for power generation from high free fatty acid (FFA) including animal and vegetable high FFA, palm oil byproduct, palm acid oil (PAO), palm sludge oil (PSO), high FFA coarse palm oil (CPO), dark oil, FFA from biodiesel glycerin acidulation, and the like, increases a processing capacity per hour with minimum energy, and facilitates management of a reaction facility. According to the present invention, to increase production efficiency of the biodiesel, the method comprises a high FFA dehydration step (S110), an esterification inducing step (S120), an acid value measurement and transfer step (S130), a biodiesel manufacturing step (S140), and a filtering step (S150).

Description

Method for manufacturing biofuel using a vacuum heating reactor}

The present invention relates to a method for manufacturing bio heavy oil using a vacuum heating reactor, and more specifically, animal and vegetable high acid value maintenance, palm oil by-product, PAO (Palm AcidOil), Palm Sludge Oil, high acid crude palm oil (High FFA CPO) For generating electricity with an acid value of 25 or less consisting of monoglyceride and diglyceride through maintaining high acid values, including dark oil and free fatty acids from biodiesel glycerin acidulation. It relates to a method for producing bio heavy oil using a vacuum heating reactor in which production of bio heavy oil is possible, treatment capacity per hour is increased with minimal energy, management of a reaction facility is easy, and production efficiency of bio heavy oil is improved.

Normally, biodiesel and bio-heavy oil are renewable eco-friendly green fuels made from bio-oil separated from animal and plant resources, and clean fuels that can significantly reduce carbon dioxide emissions because carbon dioxide generated during combustion can be absorbed through cultivation of raw crops. Can be said.

Accordingly, biodiesel is produced from bio-oil and methanol at a commercial level, and innovative technology development is continuously being attempted to improve productivity, economy, and product performance. In recent years, biodiesel mostly uses vegetable oil (rapeseed oil, soybean oil, palm oil, waste oil, etc.) as a raw material, and the ratio of the total production ratio to the raw material cost is high. There is this.

Waste oil or palm oil by-product (PFAD; palm acid oil, PAO), high FFA CPO, dark oil (dark oil) that are difficult to use for edible use to solve the problem of supply and demand instability and high cost of these raw materials ), Process development is actively underway to utilize low-fat, high-acid oils such as free fatty acids from biodiesel glycerin acidulation as raw materials for biodiesel production.

Accordingly, in the registration number 10-1847780 disclosed in the related art, (a) acid value (Acid Value) of 50 or more, based on 100% by weight of the co-catalyst, based on 100% by weight, by adding 01% to 03% by weight of 100 ℃ ~150 ℃ / 30 performing dehydration for 1 hour to 5 hours under a vacuum of mmHg or less; (b) inducing 10 to 20% by weight of unrefined glycerin relative to 100% by weight of free fatty acid while maintaining high acid value separated from moisture, and 01 to 03% by weight of 100% by weight of high acid value to induce an ester reaction; (c) after the step (b), measuring the acid value for the reactants and extracting only the oil having an acid value of 25 or less and transferring it to the precipitation tank; (d) cooling the fats and oils having an acid value of 25 or less stored in the sedimentation tank to 80° C., and dividing the cooled fats into upper and lower parts through a layer separation phenomenon by sedimentation, and extracting only bio heavy oil corresponding to the upper parts; (e) filtering the bio-heavy oil; And (f) storing the filtered bio-heavy oil.

However, the prior art requires a dehydration process to separate moisture by heating under vacuum in a state in which the high acid value is stored, and it takes at least 1 hour to 5 hours due to the characteristic of inducing a stepwise temperature rise in the dehydration process. There is a problem in that it is very difficult to secure price competitiveness and physical properties, especially because heavy oil productivity is inefficient.

KR 10-1847780 B1 (2018.04.04.)

Accordingly, the present invention has been devised to solve the above-mentioned problems, animal and vegetable high acid value maintenance, palm oil by-products, PAO (Palm AcidOil), Palm Sludge Oil, high acid crude palm oil (High FFA CPO), dark oil ( Production of bio heavy oil for power generation with an acid value of 25 or less consisting of monoglyceride and diglyceride through maintenance of high acid value including dark oil) and free glycerin separated oil (Free Fatty Acids from Biodiesel Glycerin acidulation) The object is to provide a method for manufacturing bio-heavy oil using a vacuum heating reactor in which the production capacity of bio-heavy oil is improved while the processing capacity per hour is increased with minimal energy, and the production efficiency of bio-heavy oil is improved.

In order to achieve this object, the feature of the present invention, (a) Acid value (Acid Value) of at least 50% based on 100% by weight of maintaining the high acid value Co-catalyst 0.1% by weight to 0.3% by weight to the vacuum heating reactor 100 Dehydration process is performed by vacuum heating reaction at less than ℃ ~150 ℃ / 30 mmHg, the dehydration process is sprayed to the upper surface of the evaporation disk 130, the high acid value mixture of the co-catalyst is sprayed through the spray nozzle 140, the evaporation disk ( 130) When the high acid value maintenance moves in the circumferential direction from the center of the evaporation disk 130 by the centrifugal force according to the rotational motion, a thin film is formed, and the high acid value maintenance thin film is heated by the evaporation disk 130 to vaporize and extract moisture. Maintaining the removed high acid value is separated from the evaporation disk 130 by centrifugal force and is collected through the lower discharge port 114 on the inner wall of the vacuum reaction heater 100; (b) inducing 10 to 20% by weight of unrefined glycerin relative to 100% by weight of free fatty acid while maintaining high acid value separated from moisture, and 0.1 to 0.3% by weight of catalyst relative to 100% by weight of high acid value to induce an ester reaction; (c) after the step (b), measuring the acid value for the reactants and extracting only the oil having an acid value of 25 or less and transferring it to the precipitation tank; (d) cooling the fats and oils having an acid value of 25 or less stored in the sedimentation tank to 80° C., and dividing the cooled fats into upper and lower parts through a layer separation phenomenon by sedimentation, and extracting only bio heavy oil corresponding to the upper parts; (e) filtering the bio-heavy oil; (F) storing the filtered bio-heavy oil; characterized in that it comprises a.

At this time, in step (a), the vacuum heating reactor 100 includes a reaction tank 110 having a steam discharge port 112 at the top and a foreign material discharge port 114 at the bottom, and a bell inside the reaction tank 110. It is installed in the direction and rotated by the driving unit, the heating shaft 120 is installed inside the heating unit 122, and the evaporation disk is heated by the heating shaft 120 is installed in the axial direction in the axial direction on the heating shaft 120 130, and each of the evaporation disk 130 is disposed adjacent to the rotating shaft 120, the evaporation disk 130 comprises a plurality of injection nozzles 140 for spraying high acid value maintenance on the top surface, the evaporation The disk 130 is heated to 100°C to 150°C, and is characterized in that the moisture contained in the high acid value maintaining thin film is provided to be instantaneously vaporized.

In addition, the evaporation disk 130 is formed in an upward inclination angle toward the circumferential direction, it is characterized in that the evaporation disk 130 is provided so that the circumferential movement speed of the thin film maintaining high acid value due to centrifugal force according to the rotational movement.

In addition, it is connected to a single distribution tank 150 with the injection nozzle 140 so that the amount of high acid value maintained is independently controlled by each valve 152, so that the injection amount decreases from the bottom of the reaction tank 110 toward the top. In addition, the evaporation disk 130 is characterized in that it is provided so that the diameter is gradually reduced in steps toward the top.

In addition, a plurality of scrapers 160 are provided inside the reaction tank 110 to contact foreign matter on the top surface of the evaporation disk 130 to remove foreign substances, and the scrapers 160 are connected to the orbiting arm 162 to evaporate disk 130 It is characterized in that it is provided to be pivoted in the circumferential direction from the center.

In addition, the cocatalyst is characterized in that it is an acid (Acid) consisting of any one of sulfuric acid, hydrochloric acid, phosphoric acid, citric acid, or a mixture of two or more.

In addition, the crude glycerin of step (b) has a purity of 97 to 98.5%, and the catalyst is any of sulfuric acid, hydrochloric acid, chlorosulfonic acid, p-TSA (paratoluenesulfonic acid), and MSA (methanesulfonic acid). It is characterized by being one.

In addition, in step (b), when the input of the unpurified glycerin and the catalyst is completed, an ester reaction is performed for 1 to 5 hours in a temperature range of 100° C. to 150° C., but the ester reaction is performed while raising the temperature by 10° C. per hour. Characterized in that to be made.

In addition, the step (b), the monoglyceride is characterized in that to obtain a synthetic glyceride having a ratio of 90% by weight or more and diglyceride within 10% by weight.

In addition, in step (e), primary filtration is performed through a centrifugal separator, and secondary filtration is performed by using a microfiltration device in which pores of 10 μm to 100 μm are formed in the bio-heavy oil having primary filtration. It is characterized by.

According to the above configuration and action, the present invention is a plant and animal high acid value maintenance, palm oil by-products, PAO (Palm AcidOil, palm oxidized oil), Palm Sludge Oil, high acid crude palm oil (High FFA CPO), dark oil (dark oil), recovered glycerin It is possible to produce bio-heavy oil for power generation with an acid value of 25 or less, consisting of monoglyceride and diglyceride, by maintaining a high acid value including free fatty acids from biodiesel glycerin acidulation. With the increase in the processing capacity per hour with energy, it is easy to manage the reaction equipment, and has the effect of improving the production efficiency of bio heavy oil.

1 is a flow chart schematically showing a method for producing bio heavy oil using a vacuum heating reactor according to an embodiment of the present invention.
Figure 2 is a view showing the chemical formula of the bio-heavy oil manufacturing method using a vacuum heating reactor according to an embodiment of the present invention.
Figure 3 is a block diagram showing a vacuum heating reactor as a whole of a bio heavy oil manufacturing method using a vacuum heating reactor according to an embodiment of the present invention.
Figure 4 is a block diagram showing the state of forming a thin film maintaining a high acid value by the vacuum heating reactor of the bio-heavy oil manufacturing method using a vacuum heating reactor according to an embodiment of the present invention.
5 is a block diagram showing a scraper of a method for producing bio heavy oil using a vacuum heating reactor according to an embodiment of the present invention.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

The present invention relates to a method for manufacturing bio heavy oil using a vacuum heating reactor, which maintains high animal and vegetable acid values, palm oil by-products, PAO (Palm AcidOil), Palm Sludge Oil, high acid crude palm oil (High FFA CPO), and dark oil. Of bio-heavy oil for power generation with an acid value of 25 or less, consisting of monoglyceride and diglyceride, through maintaining a high acid value, including (dark oil), recovered glycerin separated oil (Free Fatty Acids from Biodiesel Glycerin acidulation), etc. Production is possible, and the processing capacity per hour is increased with minimal energy, and it is easy to manage the reaction equipment. Meanwhile, in order to improve the production efficiency of bio heavy oil, a high acid value maintenance dehydration step (S110), an ester reaction induction step (S120) , Acid value measurement and transfer step (S130), bio-heavy oil manufacturing step (S140), filtration processing step (S150).

As shown in FIG. 1, the method for producing bio heavy oil of the present invention includes animal and vegetable high acid value, palm oil by-product, PAO (PalmAcid Oil), Palm Sludge Oil, high acid crude palm oil (High FFA CPO), dark oil ( dark oil), a high acid value maintenance dehydration step (S110) of dehydrating high acid value maintenance within a certain temperature range, including recovered glycerin separated oil (Free Fatty Acids from biodiesel glycerin acidulation).

Here, in the high acid value maintenance dehydration step (S110), 0.1 wt% to 0.3 wt% of the cocatalyst is added to the vacuum heating reactor 100 based on 100 wt% of the acid value (Acid Value) of 50 or more, and 100° C. to 150° C. Dehydration process is performed by vacuum heating reaction at less than ℃ / 30 mmHg, the dehydration process is sprayed to the upper surface of the evaporation disk 130, the high acid value of the co-catalyst is sprayed through the spray nozzle 140, the evaporation disk 130 rotates When the high acid value maintenance moves in the circumferential direction from the center of the evaporation disk 130 by the centrifugal force according to the movement, a thin film is formed, and the high acid value maintenance thin film is heated by the evaporation disk 130 to vaporize and extract moisture, and the high acid value from which moisture is removed The maintenance is a step of being separated on the evaporation disk 130 by centrifugal force and collected through the lower discharge port 114 on the inner wall of the vacuum reaction heater 100.

High acid value maintenance dehydration step (S110) is a step of removing water contained in high acid value maintenance by dehydrating high acid value maintenance of acid value (Acid Value) of 50 or more, and after inputting high acid value maintenance to the vacuum heating reactor 100, sulfuric acid, hydrochloric acid, This is a step of adding dehydration of maintaining a high acid value in a certain temperature range by adding an acid consisting of any one of phosphoric acid, citric acid, or a mixture of two or more.

Here, the present invention is preferred to use a high acid value oil having an acid value of 50 or more and 100 or less, but is not limited thereto, and it is of course possible to make the production of bio heavy oil by using a high acid value oil having a maximum acid value of 200 or less.

In addition, the acid (Acid) that is added together during dehydration of the high acid value maintenance is to perform the function of a co-catalyst, 01% to 03% by weight based on 100% by weight of the high acid value maintenance.

In FIG. 3, the vacuum heating reactor 100 is installed in the longitudinal direction inside the reactor 110 and the reaction tank 110 provided with a steam discharge port 112 at the top and a foreign material discharge port 114 at the bottom. The heating shaft 120 is rotated by the driving unit and the heating unit 122 is installed therein, and the evaporation disk 130 which is installed in the axial direction in the axial direction on the heating shaft 120 and heated by the heating shaft 120. , Each evaporation disk 130 is disposed adjacent to the rotating shaft 120, the evaporation disk 130 comprises a plurality of injection nozzles 140 for spraying high acid value maintenance on the top surface, the evaporation disk 130 Is heated to 100 ℃ ~ 150 ℃, is provided so that the moisture contained in the high acid value thin film is instantaneously vaporized.

Here, the evaporation disk 130 is connected to the heating shaft 120 is provided to be heated by conduction heat, or it is also possible to configure the evaporation disk 130 to directly heat by forming a heating wire or a steam line.

In FIG. 4, maintaining the high acid value injected through the injection nozzle 140 moves in the circumferential direction from the center of the evaporation disk 130 by centrifugal force according to the rotational motion of the evaporation disk 130 to form a thin film for maintaining the high acid value, and maintaining the high acid value The thin film is heated by the evaporation disk 130, and water is vaporized and extracted, and the high acid value from which the moisture is removed is separated from the evaporation disk 130 by centrifugal force and collected through the lower discharge port 114 of the vacuum reaction heater 100. It is provided to be processed.

Accordingly, while maintaining the high acid value inputted into the reaction tank 110 is dispersed and injected into the upper surface of each evaporation disk 130 through a plurality of injection nozzles 140, it is diffused in the circumferential direction from the center of the evaporation disk 130 by centrifugal force. Since the formation of the retaining thin film improves the efficiency of water extraction due to the vacuum heating reaction, there is an advantage that the processing capacity per hour is greatly increased by expanding the vacuum heating reaction area compared to the capacity of the vacuum reaction heater 100.

At this time, the evaporation disk 130 is formed at an upward inclination angle toward the circumferential direction. Accordingly, the evaporation disk 130 maintains a high acid value due to centrifugal force due to the rotational motion. As the moving speed of the thin film decreases in the circumferential direction, the time remaining on the top surface of the evaporation disk 130 is delayed, thereby improving the efficiency of removing water by vacuum heating reaction of maintaining the high acid value. do.

In addition, it is connected to a single distribution tank 150 with the injection nozzle 140 so that the amount of high acid value maintained is independently controlled by each valve 152, so that the injection amount decreases from the bottom of the reaction tank 110 toward the top. And, the evaporation disk 130 is provided to be gradually reduced in diameter toward the top.

Accordingly, the evaporation disk 130 is formed to gradually decrease in diameter toward the upper portion, and the evaporation disk 130 is adjusted as the supply amount of the high acid value maintained through the spray nozzle 140 is adjusted in consideration of the size capacity of the evaporation disk 130 for each layer. ) Glycerin vapor evaporated from each layer is quickly transported and discharged to the upper portion without interference to the upper layer evaporation disk 130, thereby preventing a decrease in the vacuum heating reaction due to the steam circulation failure.

In FIG. 5, inside the reaction tank 110, a plurality of scrapers 160 are provided to remove foreign substances by contacting the top surface of the evaporation disk 130, and the scrapers 160 are connected to the orbiting arm 162 to evaporate disk ( 130) It is provided to be pivoted in the circumferential direction from the center. The swinging arm 162 is installed to be swiveled by the driving unit, while the scraper 160 moves in the circumferential direction from the center of the evaporation disk 130 while the evaporation disk 130 is being rotated, thereby removing foreign matter remaining on the surface. .

At this time, since the scraper 160 is formed in a width of 5 to 10 mm and is transported in contact with the upper surface of the evaporation disk 130, a process of physically removing the adsorbed residue even while maintaining a high acid value during vacuum heating reaction is periodically performed to evaporate Since the top surface of the disk 130 is kept clean, the vacuum heating reaction efficiency is always maintained uniformly.

Subsequently, after the dehydration is completed, the high acid value is maintained, and after introducing glycerin and a catalyst, an ester reaction induction step (S120) is performed so that an ester reaction can be performed. In the ester reaction induction step (S120), unpurified glycerin (non-desorption glycerin) having a purity of 97 to 98.5% is added to maintaining a high acid value separated from moisture, and the amount of the unpurified glycerin is included in comparison with the weight of maintaining the high acid value. However, it is preferable that a certain amount of input is made in comparison with the free fatty acid included in maintaining the high acid value.

That is, the present invention can be made in a ratio of 10 to 20% by weight of unrefined glycerin relative to 100% by weight of free fatty acid during high acid value maintenance, and also compared to 500g of free fatty acid contained in high acid value maintenance, unrefined It is configured such that 50-100 g of glycerin is added.

In this case, the amount of the unpurified glycerin may vary depending on the weight of the free fatty acid contained in maintaining the high acid value.

For example, when the weight of the free fatty acid contained in the maintenance of a high acid value of 1,000 g with an acid value of 50 is 250 g, it is preferable that 25-50 g of unpurified glycerin added for the ester reaction is added.

Here, the unpurified glycerin is produced by distilling crude glycerine only, which means that a separate decolorization process has not been performed, which is more expensive than using purified glycerin in manufacturing bio heavy oil. Can be significantly reduced.

In addition, as the catalyst input for the ester reaction, any one of sulfuric acid, hydrochloric acid, chlorosulfonic acid, p-TSA (paratoluenesulfonic acid), and MSA (methanesulfonic acid) may be used, but in the present invention, p-TSA, Or it is preferable to use any one of MSA, 0.1 to 0.3% by weight based on 100% by weight of high acid value maintenance.

In the ester reaction induction step (S120) of the present invention, when the input of the unpurified glycerin and the catalyst is completed, the ester reaction is performed for 1 to 5 hours in a temperature range of 100° C. to 150° C., preferably 10° C. per hour. Let the reaction take place while heating up each time.

That is, after the ester reaction was carried out for 1 hour at a temperature of 100° C. in the reactor, the temperature was raised by 10° C. so that the ester reaction was performed for 1 hour again, and the ester reaction was performed for a total of 5 hours while heating up to 150° C. Is to make this happen.

In the present invention, monoglyceride and diglyceride are obtained through the above-described process. In particular, among the glycerides obtained, monoglyceride has a ratio of 90% by weight or more, and diglyceride is 10 It is to obtain a synthetic glyceride having a ratio within weight% so that bio-heavy oil is produced.

In addition, when the above-described ester reaction inducing step (S120) is completed, the acid value for the reactant is measured and the acid value of the oil and fat is transferred to the sedimentation tank by separating only the oil having an acid value of 25 or less.

At this time, the maintenance of an acid value of 25 or more may be performed in the reactor at a temperature of 150°C for a second ester reaction for 1 hour.

In addition, the present invention performs a step (S140) for preparing bio-heavy oil from the oil having an acid value of 25 or less transferred to the precipitation tank. In the bio-heavy oil manufacturing step (S140), a cooling step is performed to cool the oil having an acid value of 25 or less stored in the sedimentation tank to 80° C., and a layer separation step of dividing the cooled oil into upper and lower parts through a layer separation phenomenon by precipitation. And, when the layer separation is completed, it consists of a step of separating only the holding of the upper layer.

At this time, the separated lower layer part contains unreacted glycerin and foreign substances generated during the reaction or a part of the generated salt, and is separated and removed from the upper layer part.

In addition, the bio-heavy oil corresponding to the separated upper layer is transferred to a filter to perform a filtration treatment step (S150) so that the filtration treatment is performed.

The filtration treatment step (S150) separates the unreacted glycerin portion and the foreign substances generated during the reaction from the bio-heavy oil from the bio-heavy oil through the centrifugal separator, and the bio-heavy oil is formed with pores of 10㎛ ~ 100㎛ By filtration using a micro-filter device, the manufactured bio-heavy oil is purified through filtration treatment.

At this time, the filtration treatment is preferably configured to be configured to carry out filtration treatment at the same time as the transfer is configured on a plurality of transfer pipes configured to store the bio-heavy oil separated through a centrifuge in a storage tank, but is not limited thereto. .

On the other hand, the present invention may further perform a bio-heavy oil storage step (S160) to store the bio-heavy oil which has been subjected to filtration treatment in a designated storage tank and to supply a certain amount to a power generation boiler and an industrial boiler.

Through each of these steps, the present invention is capable of producing bio heavy oil for power generation with an acid value of 25 or less, consisting of monoglyceride and diglyceride.

The terms "include", "compose" or "have" as described above mean that the corresponding component can be inherent unless otherwise stated, and do not exclude other components. It should be interpreted that it may further include other components, and all terms, including technical or scientific terms, unless otherwise defined, are generally understood by those skilled in the art to which the present invention pertains. It has the same meaning as that.

100: vacuum condensation reactor 110: reactor
120: heating shaft 130: evaporation disk
140: spray nozzle 150: distribution tank
160: scraper

Claims (6)

(a) Acid value (Acid Value) 0.1% to 0.3% by weight of the co-catalyst is added to the vacuum heating reactor 100 based on 100% by weight of a high acid value of 50 or more. Vacuum heating reaction at 100°C to 150°C / 30 mmHg or less The dehydration process is performed, and the dehydration process maintains the high acid value through which the co-catalyst is mixed through the spray nozzle 140, is sprayed onto the top surface of the evaporation disk 130, and maintains the high acid value by centrifugal force according to the rotational motion of the evaporation disk 130. When moving in the circumferential direction from the center of the evaporation disk 130, a thin film is formed, and the high acid value maintaining thin film is heated by the evaporation disk 130 to vaporize and extract moisture, and maintaining the high acid value from which the moisture is removed is evaporated disk 130 by centrifugal force. ) Is separated from the top of the vacuum reaction heater 100 rides the inner wall and is collected through the lower discharge port 114;
(b) inducing an ester reaction by adding 10 to 20% by weight of unrefined glycerin to 100% by weight of free fatty acid, and 0.1 to 0.3% by weight of catalyst relative to 100% by weight of high acid value while maintaining high acid value separated from moisture;
(c) after step (b), measuring the acid value for the reactant and extracting only the oil having an acid value of 25 or less and transferring it to the precipitation tank;
(d) cooling the fats and oils having an acid value of 25 or less stored in the sedimentation tank to 80° C., and dividing the cooled fats into upper and lower parts through a layer separation phenomenon by sedimentation, and extracting only bio heavy oil corresponding to the upper parts;
(e) filtering the bio-heavy oil;
(f) storing the filtered bio-heavy oil;
In step (a), the vacuum heating reactor 100 includes a reaction tank 110 provided with a steam discharge port 112 at the top and a foreign material discharge port 114 at the bottom, and a longitudinal direction inside the reaction tank 110. The heating shaft 120 is installed and rotated by the driving unit and the heating unit 122 is installed therein, and the evaporation disk 130 installed in the axial direction in the axial direction on the heating shaft 120 and heated by the heating shaft 120 ), and each of the evaporation disk 130 is disposed adjacent to the rotating shaft 120, the evaporation disk 130 comprises a plurality of injection nozzles 140 for spraying high acid value maintenance on the top surface, the evaporation disk ( 130) is heated to 100 ℃ ~150 ℃, is provided so that the moisture contained in the high acid value thin film is vaporized instantaneously,
Inside the reaction tank 110 is provided with a plurality of scrapers 160 that are in contact with the upper surface of the evaporation disk 130 to remove foreign substances, the scrapers 160 are connected to the orbiting arm 162 and of the evaporation disk 130 Method for producing bio-heavy oil using a vacuum heating reactor, characterized in that it is provided to be pivoted in the circumferential direction from the center.
According to claim 1,
The evaporation disk 130 is formed at an upward inclination angle toward the circumferential direction, and the evaporation disk 130 is equipped with a vacuum heating reactor, characterized in that it is provided so that the moving speed of the circumferential direction of the thin film maintaining high acid value due to centrifugal force according to the rotational movement is reduced. Method for manufacturing bio heavy oil.
According to claim 1,
The injection nozzle 140 is connected to a single distribution tank 150 so that the amount of maintaining the high acid value is controlled independently by each valve 152, and the injection amount is set to decrease from the bottom of the reaction tank 110 to the top. , The evaporation disk 130 is bio-heavy oil manufacturing method using a vacuum heating reactor characterized in that it is provided to be gradually reduced in diameter toward the top.
According to claim 1,
The crude glycerin of step (b) has a purity of 97 to 98.5%, and the catalyst is any one of sulfuric acid, hydrochloric acid, chlorosulfonic acid, p-TSA (paratoluenesulfonic acid), and MSA (methanesulfonic acid). Bio heavy oil manufacturing method using a vacuum heating reactor, characterized in that.
According to claim 1,
In the step (b), when the input of the unpurified glycerin and the catalyst is completed, the ester reaction is performed for 1 to 5 hours in a temperature range of 100°C to 150°C, but the ester reaction is performed while raising the temperature by 10°C per hour. Bio heavy oil manufacturing method using a vacuum heating reactor, characterized in that.
According to claim 1,
In step (e), primary filtration is performed through a centrifugal separator, and secondary filtration is performed by using a microfiltration device in which pores of 10 μm to 100 μm are formed in the bio-heavy oil having primary filtration. Method for producing bio heavy oil using a vacuum heating reactor characterized in that.

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