KR102122055B1 - Method for manufacturing biofuel using a reactor for preventing reverse reaction - Google Patents

Abstract

The present invention relates to a method for manufacturing biodiesel using a reverse reaction-prevention 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 second esterification inducing step (S130), a biodiesel manufacturing step (S140), a filtering step (S150), and a biodiesel storage step (S160).

Description

METHOD FOR MANUFACTURING BIOFUEL USING A REACTOR FOR PREVENTING REVERSE REACTION

The present invention relates to a method for preparing bio heavy oil using a reaction preventing reaction reactor, and more specifically, 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) 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 is possible to produce bio-heavy oil, increase the positive reaction efficiency of maintaining an acid value of 25 or more through a reaction system that prevents reverse reaction, and continuously separate and process high-acid value maintenance through a specific gravity difference, thereby preventing an adverse reaction reactor that improves production efficiency of bio-heavy oil. It relates to a method for producing bio heavy oil used.

Bio-diesel and bio-heavy oil are renewable, eco-friendly green fuels made from bio-oil separated from animal and plant resources. Clean fuels that can significantly reduce the amount of carbon dioxide emitted 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 separately; (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) This is possible, by improving the positive reaction efficiency of maintaining a high acid value of 25 or more acid through a reverse reaction prevention reactor, and treating the high acid value maintenance of the layer separated by a specific gravity difference, a method for producing bio heavy oil using a reverse reaction prevention reactor that improves production efficiency of bio heavy oil The purpose is to provide.

In order to achieve this object, the features of the present invention, (a) acid value (Acid Value) of 50 or more high acid value maintained 100% by weight based on 100% by weight of the co-catalyst 0.1% to 0.3% by weight of 100 ℃ ~150 ℃ / 30 mmHg The step of performing the dehydration process in the vacuum condition below; (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), the acid value for the reactant is measured, only oils having an acid value of 25 or less are extracted and transferred to a settling tank, and oils having an acid value of 25 or more are introduced into a reaction preventing reactor (1) to induce a secondary ester reaction. And, in the secondary ester reaction, the reactant sucked through the circulation inlet 32 is sprayed upward from the lower portion of the inner tank 20 using the circulation outlet 34, and the reactant collides with the stirring blade 22 As it is atomized and moved downward, it is moved to the inner space of the outer tank 10 through the lower flow path 24 of the inner tank 20, and the reactants moved to the outer tank 10 are formed by the outer slope tube 16. A step of collecting and holding the separated powders and fractions by the difference in specific gravity through the flow path 26 through the upper port 14 and the lower port 12, respectively; (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 separately; (e) filtering the bio heavy oil; (f) storing the filtered bio-heavy oil; characterized in that it comprises a.

At this time, the co-catalyst is characterized in that the 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 the step (c), the reactor 1 for preventing a reverse reaction is discharged from the lower port 12 from which a product having a relatively high specific gravity among impurities and a layer separated by a specific gravity difference is discharged, and a product having a relatively low specific gravity discharged. An outer tank 10 provided with an upper port 14 to be provided, and an agitation blade 22 provided inside the outer tank 10, and a lower flow path 24 communicating with the outer tank 10 at the bottom The inner tank 20 is formed, the inner tank 20, the inlet circulating 32 to suck the reactants in the upper region, and the reactant sucked through the circulating inlet 32 upward from the bottom of the inner tank 20 A multi-tube 40 which is provided to supply a reactant by being connected to a reactant circulating portion 30 and a circulating outlet 34 composed of a circulating outlet 34 to be injected with a circulating pump 36 circulating the reactants It characterized in that using a chemical reaction is made, and the reaction is layer separated by a specific gravity difference.

In addition, the outer tank 10 capacity is characterized in that it is formed in a size increased by 2 to 5 times compared to the inner tank 20 capacity.

In addition, the reactant is sprayed upward from the inner tank 20 through the circulating outlet 34, and the reactants collide with the stirring blade 22 and move downward while being atomized, thereby moving the inner tank 20 to the lower flow passage 24. Through the outer tank 10 is moved to the inner space, the reactant moved to the outer tank 10 is characterized in that the oil and the impurities are layered by the difference in specific gravity as the flow rate decreases.

In addition, an ejector 50 is installed in the circulation outlet 34, and the ejector 50 is provided to mix and spray the reactants circulated through the reactant circulation unit 30 and the new reactants supplied through the multi-pipe 40. It is characterized by being.

In addition, in the lower space of the outer tank 10, an outer inclined tube 16 in which the size is reduced toward the upper portion is installed, and an upper flow path in which the inner tank 20 and the gap are reduced in size toward the upper portion of the outer inclined tube 16 ( 26) is formed, the reactant passing through the upper flow path 26 is characterized in that the flow rate is lowered and is provided so that the maintenance and impurities are layer-reacted by the specific gravity difference.

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 having a pore size of 10 μm to 100 μm are formed for 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 high acid value including free fatty acids from biodiesel glycerin acidulation, and preventing adverse reactions. Through the reactor, the positive reaction efficiency of maintaining an acid value of 25 or more is increased, and the production efficiency of bio-heavy oil is improved by continuously separating and treating the acid value with oil and impurities.

1 is a flow chart schematically showing a method for producing bio-heavy oil using an anti-reaction 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 of the bio-heavy oil using a reaction reaction prevention reactor according to an embodiment of the present invention.
Figure 3 is a block diagram showing the overall reaction to prevent the reaction of the bio-heavy oil manufacturing method using a reaction preventing reactor according to an embodiment of the present invention as a whole.
Figure 4 is a block diagram showing the reactant circulating injection state of the reaction to prevent reverse reaction of the bio-heavy oil manufacturing method using a reverse reaction prevention reactor according to an embodiment of the present invention.
5 is a conceptual diagram of a biodiesel reaction system according to the prior art.

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. (biomass), which is composed of monoglyceride and diglyceride through high acid value maintenance, including dark oil and free fatty acids from biodiesel glycerin acidulation. In order to improve the production efficiency of bio-heavy oil by enabling production, increasing the positive reaction efficiency of maintaining an acid value of 25 or more via the reactor 1 for preventing reverse reaction, and treating the oil of high acid value by separating it into fat and impurities using a specific gravity difference. High acid value maintenance dehydration step (S110), ester reaction induction step (S120), acid value measurement and secondary ester reaction induction step (S130), bio heavy oil production step (S140), filtration treatment step (S150), and bio heavy oil storage step (S160) ).

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 dehydration step of maintaining the high acid value (S110), 0.1 wt% to 0.3 wt% of the cocatalyst is added based on 100 wt% of the acid value (Acid Value) of 50 or more and vacuum is performed at 100°C to 150°C / 30 mmHg or less This is a step in which the dehydration process is performed by a heating reaction.

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.

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 input at a ratio of 10 to 20% by weight of unrefined glycerin relative to 100% by weight of free fatty acid during maintenance of high acid value, and also, compared to 500g of free fatty acid included in maintaining high acid value, unrefined glycerin 50 to It is configured to make 100 g of input.

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 induction step (S120) is completed, the acid value for the reactant is measured, and only the oil having an acid value of 25 or less is separated and transferred to the precipitation tank, and the maintenance of the acid value of 25 or more is introduced into the reactor for preventing reverse reaction 2 The acid value measurement to induce the secondary ester reaction and the secondary ester reaction induction step (S130) are performed.

Here, the maintenance of the acid value of 25 or more is introduced into the reaction preventing reactor (1) to induce an ester reaction, and in the secondary ester reaction, the reactant sucked through the circulation inlet (32), the inner tank (20) using the circulation outlet (34) ) Is injected upward from the lower part, the reactant is collided with the stirring blade 22 and moved downward while being atomized and moved to the inner space of the outer tank 10 through the lower flow path 24 of the inner tank 20, The reactants transferred to the outer tank 10 pass through the upper flow path 26 formed by the outer inclined pipe 16, and the flow rate is lowered, and the separated and maintained impurities separated by the specific gravity difference are respectively transferred to the upper port 14. And collecting processing through the lower port 12.

Subsequently, in the reverse reaction prevention reactor 1 according to the present invention, the inner tank and the outer tank in which the reactants are layer-separated by specific gravity difference are compactly improved in a double structure to improve the forward reaction efficiency and bio-formation formed in the layer separation reaction of the product. It consists of an outer tank 10, an inner tank 20, a reactant circulation section 30, and a multi-tube 40 to continuously operate for a long time while continuously discharging heavy oil and impurities.

The outer tank 10 according to the present invention includes a lower port 12 through which a product having a relatively high specific gravity is discharged from a product separated by layer separation in maintaining a high acid value, and an upper port 14 through which a product having a relatively low specific gravity is discharged. ) Is provided, and the outer tank 10 is divided into an inner space and an outer space by an inner tank 20 whose inner space will be described later.

In addition, the inner space and the outer space are communicated by the lower flow path 24, wherein the inner space is vortexed by the stirring blade 22, while the outer space is formed larger than the inner space to induce a decrease in flow velocity. The reactants are provided to separate the layers by specific gravity difference.

In addition, the inner tank 20 according to the present invention is installed inside the outer tank 10 is provided with a stirring blade 22, the lower flow path 24 is formed in communication with the outer tank 10 at the bottom. The inner tank 20 is disposed on a concentric circle with the outer tank 10, wherein the outer tank 10 has a size that is increased by 2 to 5 times compared to the inner tank 20, and the inner tank 20 When the reactants that are stirred in the inside moves to the inside of the outer tank 10 through the lower flow passage 24, the flow rate is reduced.

In addition, the stirring blade 22 is installed on the inner tank 20, and is provided to circulate the reactant sprayed upward through the circulation outlet 34, which will be described later.

In addition, the reactant circulation unit 30 according to the present invention includes a circulation inlet 32 for sucking the reactants from the upper region of the inner tank 20, and a reactant sucked through the circulation inlet 32 at the lower portion of the inner tank 20. It is composed of a circulating outlet (34) for injecting upwards and a circulation pump (36) for circulating reactants.

That is, the reactant circulation unit 30 has a circulating structure in which a reactant is sucked into the upper region of the inner tank 20 and supplied to the lower region of the inner tank 20, wherein the circulating outlet 34 is an outer tank 10 ) It extends from the bottom surface to the center height of the inner tank 20.

Accordingly, since the reactant sprayed through the circulation outlet 34 is moved downward in an agitated (micronized) state by the stirring blade 22, the forward reaction efficiency is improved.

In addition, the multi-pipe 40 according to the present invention is connected to the circulating outlet 34 to provide a new reactant. The amount of new reactant input and the time of input through the multi-pipe 40 are set by the control unit.

In operation, the reactant is sprayed upward from the lower portion of the inner tank 20 through the circulation outlet 34, and the reactant collides with the stirring blade 22 and moves downward while being atomized and flows downward. (24) is moved to the outer space through the outer tank (10), and the reactants transferred to the outer tank (10) are formed in the lower layer due to a relatively high specific gravity among impurities and impurities separated by layers due to a difference in specific gravity. The product is collected and discharged through the lower port 12 downward, and the product formed on the upper layer is collected and discharged through the upper port 14 due to its relatively high specific gravity. Then, the discharge amount discharged through the upper port 14 and the lower port 12 is measured, and a corresponding amount of new reactant is introduced.

As described above, the inner tank 20 in which the reactants are positively reacted and the outer tank 10 in which the reactants are layered by a specific gravity difference are compactly improved in a dual structure, thereby improving the forward reaction efficiency and bio heavy oil in the product layer separation reaction. It has the advantage of continuously operating for a long time while continuously separating and discharging and impurities.

In FIG. 4, an ejector 50 is installed at the circulation outlet 34, and the ejector 50 mixes and sprays reactants circulated through the reactant circulation unit 30 and new reactants supplied through the multi-pipe 40. It is provided as possible. The ejector 50 is connected to a multi-pipe 40 in an internally constricted region, and when a reactant is injected through the circulation outlet 34, a new reactant is sucked through the multi-pipe 40 and atomized, so that the reactant is mixed and sprayed. After moving into the outer tank 10, the reaction efficiency of layer separation due to the difference in specific gravity is improved.

In addition, in the lower space of the outer tank 10, an outer inclined tube 16 in which the size is reduced toward the upper portion is installed, and an upper flow path in which the inner tank 20 and the gap are reduced in size toward the upper portion of the outer inclined tube 16 ( 26) is formed, and the reactants that have passed through the upper flow passage 26 are provided so that the separated oils and impurities are layer separated by the difference in specific gravity while the flow rate is lowered.

Reaction prevention reactor 1 according to the present invention does not install a separate separation device such as a reaction system combined with a reactor and a layer separator in the prior art shown in FIG. 5, so that facility cost and maintenance cost are reduced, and reaction of reactants and The process of separating the products may be performed at the same time, and two or more products generated by the reaction may not be layer-separated due to interference due to a circulating action, and may be mixed to solve the problem that the separation efficiency due to the specific gravity difference is greatly reduced.

In addition, according to the above, while the reactant inside the inner tank 20 moves to the outer tank 10 side through the lower flow path 24, a pipeline resistance is generated by the outer inclined pipe 16, and the reactant movement is delayed. As it flows through the upper flow passage 26 and expands, the flow rate decreases, and the separation efficiency of oil and impurities separated by specific gravity difference improves.

On the other hand, a heater is installed inside the inner tank 20, and the reactants heated inside the inner tank 20 by the heater are thermally protected by the outer tank 10 and maintained at a uniform temperature, so that the positive reaction efficiency and quality are maintained. Is improved.

As an example, the reaction was prepared in a ratio of [soybean oil 1,000g, methanol 200g, NaOCH3 (70% by weight methanol + 30% by weight NaOCH3) 10g].

First, 1 liter of the reactants are injected into the reactor, the temperature is raised to 50° C., and then the circulation pump is operated to self-circulate 1 ℓ/Hr, 2 ℓ/Hr. It was set to 32 l/Hr, and the reaction time was 20 minutes. As a result, when the reactor according to the present invention was externally circulated at an appropriate flow rate, a BD (biodiesel) conversion rate close to about 90% could be obtained within 15 minutes of starting the reaction, and a BD conversion rate reached about 97% when reacted for 25 minutes.

As described above, using the specific gravity difference of the reactant generated through the acid value measurement and the second ester reaction induction step (S130), the layer is separated into fats and oils, and the layered bio heavy oil and impurities are continuously discharged. While it is possible to operate continuously for a long time, there is an effect that the forward reaction efficiency is improved through the reactor 1 for preventing reverse reaction.

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 the step (S140) of preparing the bio heavy oil from the maintenance of the acid value of 25 or less transferred to the precipitation tank through the acid value measurement and the second ester reaction induction step (S130). 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, consists 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 process (S150) so that filtration 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 μm to 100 μm. Filtering is performed using a micro-filter device, so that the manufactured bio-heavy oil is purified through filtration.

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) for storing the bio-heavy oil that has been subjected to filtration treatment in a designated storage tank and supplying 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.

1: Reaction prevention reactor 10: Outer tank
20: inner tank 30: reactant circulation section
40: multi tube 50: ejector

Claims (6)

In the method for producing bio-heavy oil using a reverse reaction prevention reactor for producing a bio-heavy oil for generating electricity having an acid value of 25 or less consisting of monoglyceride and diglyceride through maintaining a high acid value,
The counter reaction prevention reactor 1 includes an outer tank 10 having a lower port 12 through which a relatively high specific gravity of the reactants separated from the layer is discharged, and an upper port 14 through which a reactant having a low specific gravity is discharged; and
An inner tank 20 including a stirring blade 22 installed inside the outer tank 10 to atomize reactants and a lower flow passage 24 provided on a lower surface of the tank to communicate with the outer tank 10 ;Wow
A circulation inlet 32 for sucking the reactants from the upper region of the inner tank 20, and a circulation outlet 34 for injecting the reactants sucked through the circulation inlet 32 upward from the bottom of the inner tank 20 And, the reactant circulating portion 30 comprising a circulation pump 36 to allow the reactant to circulate inside the outer tank 10 and the inner tank 20; And
A multi-pipe 40 connected to the reactant circulation unit 30 and the circulation outlet 34 to supply new reactants; and
It comprises a; ejector 50 is installed in the circulating outlet (34) for mixing and spraying the reactant circulated through the reactant circulation unit 30 and the new reactant supplied through the multi-tube 40;
In the lower space of the outer tank 10, an outer inclined pipe 16 is reduced in size as it goes upward, and the outer inclined pipe 16 is an upper flow path in which the gap is reduced from the inner tank 20 as it goes to the upper end. The reactant that has been formed (26) and passes through the upper flow passage (26) is separated into layers of oil and fat by the difference in specific gravity in a state in which the flow rate is lowered.
The capacity of the outer tank 10 is formed in a size increased by 2 to 5 times compared to the capacity of the inner tank 20, and moved from the inner tank 20 through the lower flow path 24 into the outer tank 10. It is configured to decrease the flow rate of the reactants,
The reverse reaction prevention reactor (1) is (a) acid value (Acid Value) of 50 or more, maintaining the high acid value based on 100% by weight of 0.1 to 0.3% by weight of the co-catalyst, 100 ℃ ~150 ℃ / 30 mmHg or less under vacuum conditions Dehydration is performed;
(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 the step (b), the acid value for the reactant is measured, only oils having an acid value of 25 or less are extracted and transferred to a settling tank, and oils having an acid value of 25 or more are introduced into a reaction preventing reactor (1) to induce a secondary ester reaction. And, in the secondary ester reaction, the reactant sucked through the circulation inlet 32 is sprayed upward from the lower portion of the inner tank 20 using the circulation outlet 34, and the reactant collides with the stirring blade 22 As it is atomized and moved downward, it is moved to the inner space of the outer tank 10 through the lower flow path 24 of the inner tank 20, and the reactants moved to the outer tank 10 are formed by the outer slope tube 16. A step of collecting and holding impurities separated from the layer by a difference in specific gravity in a state in which the flow rate passes through the flow path 26 through the upper port 14 and the lower port 12, respectively;
(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 separately;
(e) filtering the bio heavy oil;
(f) storing the filtered bio-heavy oil; a method for producing bio-heavy oil using a reaction preventing reaction reactor comprising the steps of:
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). Method for producing bio-heavy oil using a reactor for preventing reverse reaction, 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. Composed,
Method for producing bio-heavy oil using an anti-reaction reaction reactor, characterized in that the monoglyceride obtains a synthetic glyceride having a ratio of 90% by weight or more and 10% by weight of diglyceride.
According to claim 1,
In the step (e), primary filtration is performed through a centrifugal separator, and secondary filtration is performed by using a micro filter device having pores of 10 μm to 100 μm for bio heavy oil having primary filtration. Method for producing bio-heavy oil using a reaction preventing reaction reactor characterized in that. delete delete

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