KR101418283B1 - Fatty acid production using waste cooking device - Google Patents

Abstract

The present invention relates to a fatty acid producing apparatus using waste cooking oil which produces fatty acids that are raw materials for a detergent, a paint, biofuel and etc., by refining liquid waste cooking oil and fat/oil residues. The fatty acid producing apparatus using waste cooking oil comprises: a raw material containing part which contains liquid waste cooking oil and fat/oil residues; a steam supplying part which supplies steam; a sulfate containing part which supplies sulfate using a sulfate injection pump; a reaction part which conducts a reaction of the raw materials, the steam, and the sulfate to separate fatty acids in a upper layer, sludgy in a middle layer, and waste water in a lower layer; a refining part comprising a first refining part and a second refining part to refine the separated fatty acids; and a final containing part which contains the refined fatty acids.

Description

[0001] The present invention relates to a fatty acid production using waste cooking oil,

The present invention relates to a process for purifying waste cooking oil and its vegetable oil residues in the liquid wastes generated from waste cooking oil and vegetable oil processing companies in the whole country to produce fatty acid which is an intermediate recyclable raw material such as detergent, paint, and biofuel, And also relates to an apparatus for producing fatty acid by using waste cooking oil so as to meet the environmental aspect of resource recycling.

Today 's modern society is in a time of urgent need for a new paradigm that satisfies both sides of the development of alternative fuels as the environmental pollution problem due to the use of petroleum resources and the crisis of depletion of petroleum resources are heightened.

It is necessary to pay attention to the waste cooking oil and other animal and vegetable oil keeping as a raw material which can satisfy economically and desperately in such a harsh environment.

However, waste edible oil and other vegetable oils have a specific gravity smaller than that of water, and some types of waste cooking oil have a property of curing. When discharged through a sewer, pipes are clogged due to hardening, or after flowing into streams or rivers It forms an oil film on the water and blocks the supply of oxygen from the outside air to the water, which threatens aquatic ecosystems including aquatic life.

In recent years, waste cooking oil is collected and recycled in various ways, which is largely used as detergent or biofuel.

First of all, one of the recycled products using waste cooking oil is soap. Usually, at home, waste cooking oil and caustic soda water are mixed and poured into a mold, and after 10 days or more, saponification reaction is performed and natural curing can be used as soap.

However, since the soap made by this method has a characteristic that it can be easily retracted in the surrounding moisture, the shape is easily deformed when it is held by hand, so it is usually difficult to use, so it is usually only used in a case. It is limited to use only.

Therefore, in order to expand the soap area for laundry or toilet soap, there is a demand for a manufacturing technique that can reduce the manufacturing process time without being easily reluctant to moisture.

In addition, when soap is produced from waste cooking oil, the unpleasant odor inherent in the waste cooking oil is caused, and improvement is required. As such conventional technologies for recycling with soap, Patent Registration No. 321105 and Patent Registration No. 313083 exist.

Next, bio-fuels include bioethanol, methanol, biodiesel, and methane gas. Biodiesel produced from animal fats, vegetable fuels, or regenerated fuels is used as fuel for vehicles , Which is the most widely used fuel for diesel engines.

The biodiesel is environmentally friendly and has no problem of exhaustion of resources. Also, since the biodiesel can be used directly in existing vehicles and can be supplied from a currently installed gas station, no infrastructure is required. Biodiesel, which can be produced by the esterification of vegetable oil, is much lower in emissions of environmental pollutants than diesel oil, and has been put into practical use since the early 1990s in the EU and the United States as vehicle fuel. At present, biodiesel produces edible oil from oil crops as a raw material. As a result, about 70% of the total production cost of bio-diesel is raw material cost. Therefore, in order to lower the production cost of biodiesel, it is necessary to secure cheaper raw materials. In particular, considering that there is little production of edible oil in Korea, there is a problem that raw materials should depend on overseas resources as well as oil to produce biodiesel.

A conventional technique for solving this problem is disclosed in Korean Patent Publication No. 99-16818 entitled " Method for manufacturing automobile fuel using waste cooking oil ", in which the regenerated fuel and the existing diesel oil are separated from the vehicle and used as vehicle fuel. In a way that was inspired before it was enacted,

Since equipment is required to be installed and used, there is a need for a separate installation cost, so that the economical efficiency is lost. Further,

Korean Patent Laid-Open Publication No. 2002-34712 entitled " Method for producing vegetable fuels for internal combustion engines using rice bran oil and waste cooking oil ", " Primary ester reaction - Secondary ester reaction - Separation of crude glycerin - Production of methyl ester - Washing, dehydration - Ester recovery '

First, the production process of the renewable fuel is a multistage process in seven stages.

Second, the production facilities and methods are complicated, for example, in the case of the first ester reaction, the reaction is carried out using vaporized methanol as a solvent.

Third, after washing the container solvent and the basic catalyst during the wash / dewatering process, the method for treatment of wastewater and the additional wastewater treatment facility will be necessary.

In the case of the above production method, it will be burdensuch for equipment costs for each process to secure a complicated process, securing the site for the production facility, etc., and the cost of wastewater treatment should be taken into account during the washing, dehydration and distillation processes. It is expected.

Korean Patent Laid-Open Publication No. 2002-34712 entitled "Apparatus for regenerating waste oil with fuel"

First, the production process is a multistage process in seven stages.

Second, after esterification, glycerin and methyl ester are separated by natural precipitation method. I wonder whether it is possible to obtain an effective yield by natural separation method, and whether the natural precipitation method is effective for long production time.

Third, adsorbent and other impurities are aggregated by adding an adsorbent to induce adsorption of impurities by adding impurities while removing impurities from methyl ester, and then adsorbing agent and other impurities are aggregated. Then, the adsorbent and flocculant are removed after layer separation by specific gravity difference, , It is expected that product production time will become longer with separation method by natural precipitation or separation of sediment layer by specific gravity difference and it is expected that after processing only the upper layer organic layer, There is a problem that it is not practically utilized because it is uncertain whether it is possible to produce an economical product or a high-purity product.

As a way to solve these problems, it is very important to utilize the waste cooking oil produced in Korea as raw material for biodiesel. Compared to the necessity of the waste cooking oil, the conventional technology contains various impurities unlike the cooking oil extracted from the maintenance plant, and as a result, it directly causes a deterioration in the quality of the biodiesel production. Although various patents and papers have been published, the conventional production methods have a disadvantage of producing biodiesel which is inferior to the quality standard due to low production yield, low purity, high filter clogging point and high pour point.

On the other hand, as the consumption of fried foods and the like has increased in recent years, the generation of waste oil of the vegetable oil used for cooking them is also increasing. The above-mentioned waste oil has a biological oxygen demand (BOD) of about 1,000,000 ppm, which is significantly higher than 35,000 ppm of miso stew and is more than 200,000 times higher than the 5 ppm that fish can survive. Therefore, It is becoming a cause.

Therefore, biodiesel produced using the vegetable oil as an alternative fuel is required to be developed in terms of resource recycling and environmental preservation.

The vegetable oil is composed of glyceride which is a fatty acid ester of glycerol together with fatty acid and glycerol. Because the vegetable oil is very difficult to use as a fuel because of its high viscosity, fatty acid methyl esters and glycerin are obtained by using methanol, which is cheaper than oil and alcohols. The fatty acid ester production method includes a direct ester method and an ester exchange method.

The direct ester method is the most common method using the reaction of RCOOH + R'OH → RCOOR` + H2O. It is the most common method to heat the fatty acid and alcohol under high temperature without reaction at 135 ℃ ~ 250 ℃ or the sulfuric acid, phosphoric acid, alkali metal acetate, sulfate , Chlorides, oxides, para-toluene, and sulfonic acid as catalysts under mild conditions.

On the other hand, in the ester exchange method, an ester exchange reaction, which is a reaction in which a fatty acid, an alcohol or an ester is reacted at 60 ° C to 80 ° C according to an ester such as triglyceride to another kind of ester, is used. In particular, the reaction between an ester and an alcohol is called an alcoholysis, and an alkali catalyst such as sodium methoxide is used.

Most of the above-mentioned reaction steps are subjected to an esterification reaction. However, such a reaction mechanism has disadvantages in that water can be generated, a subsequent treatment device for removing the catalyst due to the use of a large amount of catalyst is required, and the efficiency and economical efficiency are low.

For example, Korean Laid-Open Patent Publication No. 99-16815 and Korean Laid-Open Patent Publication No. 1999-79052 disclose a method of regenerating a waste cooking oil to produce an alternative fuel, The cost of using water and the costs of wastewater treatment are high.

Accordingly, the present invention can purify waste vegetable oil and vegetable oil residues to produce fatty acid which is an intermediate recyclable raw material such as detergent, paint, and biofuel, thereby reducing the waste disposal cost and also contributing to environmental aspects such as resource recycling. And an object of the present invention is to provide a fatty acid producing apparatus using the same.

In order to achieve the above object,

"A raw material storage unit that stores the liquid waste oil and the vegetable oil residues generated from the vegetable edible oil preservation processing company in a storage tank for 84 hours to 88 hours after collecting and transporting them using a transportation vehicle, A steam supply unit for mixing the raw material discharged from the raw material storage unit and supplying steam at a temperature of 90 ° C generated through a steam boiler, and a steam supply unit for mixing the raw material discharged from the raw material storage unit, % Of sulfuric acid by using an injection pump, and a raw material discharged from the raw material storage part, steam stream supplied from the steam supply part, and sulfuric acid supplied from the sulfuric acid storage part, A reaction part in which the upper part is separated into fatty acid, the middle part is separated into sludge and the lower part is separated into waste water, and the separated fatty acid As consisting of the first purifying unit and the first to re-purification of the purified fatty acids in the purification unit and the second purification unit consisting of parts of tablets, for final storage portion for storing the fatty acid purified by the purification unit for purifying,

Each of the storage tanks is provided with an inlet valve at a sub-pipe for storing a raw material flowing through a main pipe at an upper center thereof, and a discharge pipe for discharging the raw material by opening and closing a discharge valve And,

The reaction tank is equipped with a fatty acid discharge valve for discharging the fatty acid formed in the upper layer, a sludge discharge valve for discharging the sludge formed in the middle layer, and a sludge discharge valve for discharging the wastewater from the lower layer in the state of being separated into the upper layer, middle layer, And the sludge discharged to the sludge discharge valve is transferred to the concentration tank of the wastewater treatment plant and the wastewater discharged to the wastewater discharge valve is discharged to the wastewater treatment plant However,

An ejector is provided at a position where the raw material discharged from the raw material storage unit and the steam stream supplied from the steam supply unit are mixed,

A static mixer for mixing the raw material discharged from the raw material storage part, the steam heat supplied from the steam supply part and the sulfuric acid supplied from the sulfuric acid storage part,

The inside of the first and second tablets is provided with a steam coil which maintains at 45 ° C, and each of them is refined for 8 hours. After the refining, the fatty acid activity is formed and separated into upper layer, middle layer and lower layer, To be transferred to the final storage section by a transfer pump provided on the outside,

A steam coil for maintaining a temperature of 45 ° C is provided in the final storage portion,

The raw material storage unit, the sulfuric acid storage unit, the reaction unit, the purification unit, and the final storage unit are each provided with a gas outlet,

Wherein the ejector has a cylindrical shape, a main hole is formed at an inner center thereof, and a plurality of partition walls are formed on the outer periphery of the main hole to form a sub-hole, and a guide plate for accelerating a flow velocity is integrally provided outside the sub- And the above object can be achieved by using the constitutional characteristic.

The present invention having the above-described constitution can be used not only to reduce the waste disposal cost but also to reduce the disposal cost of raw materials such as detergents, paints, biofuels and the like by refining the waste cooking oil and the vegetable preservation residues with a single batch device It is possible to exert an effect of meeting the environmental aspect of recycling.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is clearly understood that the same is by way of illustration and example only and is not to be construed as limited to the embodiments set forth herein. Various changes and modifications may be made by those skilled in the art.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is an overall schematic view of a fatty acid producing apparatus using waste cooking oil of the present invention;
2 is a detailed view of a raw material storage portion in a fatty acid production apparatus using waste cooking oil according to the present invention,
FIG. 3 is a detailed view of a steam supply unit, a sulfuric acid storage unit, and a reaction unit in a fatty acid production apparatus using waste cooking oil according to the present invention;
4 is a detailed view of an ejector in a fatty acid production apparatus using waste cooking oil according to the present invention,
FIG. 5 is a detailed view of the purification unit and the final storage unit in the fatty acid production apparatus using the waste cooking oil of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, an apparatus for producing fatty acid using waste cooking oil according to the present invention will be described in detail with reference to the drawings.

FIG. 2 is a detailed view of a raw material storage unit in a fatty acid production apparatus using the waste cooking oil according to the present invention. FIG. 3 is a schematic view showing a fatty acid production apparatus using waste cooking oil according to the present invention 4 is a detailed view of an ejector in an apparatus for producing fatty acid using waste cooking oil according to the present invention, and Fig. 5 is a diagram showing the details of an ejector in the apparatus for producing fatty acid using waste cooking oil according to the present invention. And a final storage section.

As shown in FIGS. 1 and 2, the indicator S1 indicates a raw material storage unit. The indicator S1 is used to collect the liquid waste oil and the vegetable oil residue generated in the vegetable oil preservation processing company using the transportation vehicle (C) And stored in a total of three storage tanks 100 for 84 hours to 88 hours, respectively,

In each of the storage tanks 100, an inlet valve 103 is provided in a sub-pipe 102 for storing a raw material flowing through a main pipe 101 at an upper center, And a discharge pipe 105 for discharging by opening and closing the discharge valve 104 for discharging.

As shown in FIGS. 1 and 3, the indicator S2 is for mixing the raw material discharged from the raw material storage unit S1 as shown in FIG. 1 and FIG. 3. The indicator S2 is a steam column of 90.degree. C. generated through the steam boiler 200 . In this case,

As shown in FIG. 1 and FIG. 3, the indicator S3 indicates a sulfuric acid storage unit, which is used to mix the raw material discharged from the raw material storage unit S1. The sulfuric acid storage tank 300 is filled with 98% And is supplied by using a pump 310. Fig.

As shown in FIG. 1 and FIG. 3, the indicating symbol S4 designates a reaction part. The indication symbol S4 indicates the raw material discharged from the raw material storage part S1, the steam column supplied from the steam supplying part S2, Sulfuric acid supplied from the reactor 400 is stirred and reacted for 8 hours with a stirrer 410 provided in the reaction tank 400 to separate the fatty acid from the upper layer, the sludge from the middle layer, and the waste water from the lower layer.

In order to discharge the fatty acid formed in the upper layer, the fatty acid discharge valve 401 is disposed in the reaction tank 400 to separate the upper layer, the middle layer and the lower layer by the stirrer 410. In order to discharge the sludge formed in the middle layer, A waste water discharge valve 403 for discharging wastewater is formed in the lower portion of the waste water discharge valve 401. The fatty acid discharged through the fatty acid discharge valve 401 is transferred to the refining portion S5, 402 is transferred to a concentration tank (not shown) of the wastewater treatment plant and the wastewater discharged to the wastewater discharge valve 403 is discharged to a wastewater treatment plant (not shown).

3, the ejector 210 is disposed at a position where the raw material discharged from the raw material storage S1 and the steam supplied from the steam supply S2 are mixed,

In addition, a static mixer 320 is provided for mixing the raw material discharged from the raw material storage unit S1, the steam heat supplied from the steam supply unit S2, and the sulfuric acid supplied from the sulfuric acid storage unit S3.

4, the ejector 210 has a cylindrical shape with a main hole 211 formed at an inner center thereof and a plurality of partitions 212 formed at an outer periphery of the main hole 211, And an induction plate 214 for accelerating the flow velocity is integrally provided outside the sub-hole 213.

As shown in FIG. 1 and FIG. 5, the indicator S5 indicates a refining unit. The refining unit 500 includes a first refining unit 500 and a second refining unit 510. First, And a second refining unit 510 for refining the refined fatty acid in the first refining unit 500. The first refining unit 500 refines the purified fatty acid.

A steam coil 520 is kept inside the first and second purification units 500 and 510 to maintain the temperature of 45 ° C. Each of the cells is refined for 8 hours. After the purification, the fatty acid activity is formed, And is transferred to the final storage unit S6 described below by the transfer pump 530 provided outside the second tablet unit 510. [

The indicator S6 indicates the final storage unit. As shown in FIG. 1 and FIG. 5, the indicator S6 stores the purified fatty acid through the purification unit S5,

The steam coil 600 is kept inside the final storage unit S6 at 45 ° C.

As shown in FIGS. 2, 3 and 5, each of the raw material storage section S1, the sulfuric acid storage section S3, the reaction section S4, the purification section S5, And a gas outlet 700 for discharging a gas such as a malodor generated in the process of treating the gas in the process of treating the gas to the malodor removing device not shown in the figure.

The reference character P indicates the raw material feed pump.

The operation relationship of the present invention having the above-described structure will now be described.

The main piping 101 and the sub piping 102, the inflow valve 103, and the main piping 102 are collected by transporting waste liquid cooking oil and vegetable oil residues, which are generated in the vegetable food preserving processing company, Is stored in each of the storage tanks 100 and stored in the storage tanks 100 for 84 hours to 88 hours, i.e., 3 days and 12 hours to 3 days and 16 hours, respectively. The odor is discharged to the gas outlet 700. After passing through the storage time as described above, the discharge valve 104 is opened, the raw material feed pump P is operated as shown in FIG. 2, and stored through the main pipe 101 The raw material is discharged and transferred from the sulfuric acid storage tank 300 of the sulfuric acid storage unit S3 after mixing in the ejector 210 and the steam heat of 90 ° C generated through the steam supply unit S2 as shown in FIG. The sulfuric acid is supplied to the static mixer 320 When the mixture is mixed and then introduced into the reaction tank 400 of the reaction unit S4, the stirrer 410 provided in the reaction tank 400 reacts for 8 hours.

When the agitation reaction is performed through the agitator 410, the fatty acid is separated in the upper layer by 20%, the sludge in the middle layer is separated by 10%, and the waste water is separated by 70% in the lower layer. In this state, And the sludge is transferred to the concentration tank of the wastewater treatment plant through the sludge discharge valve 402. The fatty acid formed in the remaining upper layer is discharged through the fatty acid discharge valve 401 to the purification section S5.

At this time, the odor generated in the sulfuric acid storage part (S3) and the reaction part (S4) is discharged to the gas outlet (700).

The fatty acid that has passed through the reaction part S4 as described above is introduced into the first refining part 500 of the refining part S5 shown in FIG. 5, and the first refining part 500 is provided with a steam coil And is then conveyed to a second refining unit 510 equipped with a steam coil 520 maintaining the temperature of 45 ° C. and refined for 8 hours. Finally, The fatty acid purified by the steam coil 600 stored in the final storage unit S6 and maintained at 45 DEG C in the final storage unit S6 is stored and stored in the storage unit S6, The period can be 18 days, and the stored fatty acids are supplied as raw materials for detergent, paint, biofuels, etc., thereby reducing waste disposal costs and meeting the environmental aspect of resource recycling.

100: Storage tank 101: Main piping
102: sub-piping 103: inflow valve
104: exhaust valve 105: exhaust pipe
200: Steam boiler 210: Ejector
211: main ball 212: partition wall
213: sub ball 214: induction plate
300: sulfuric acid storage tank 310: injection pump
320: Static mixer 400: Reactor
401: Fatty acid discharge valve 402: Sludge discharge valve
403: Wastewater discharge valve 410: Stirrer
500: first refining unit 510: second refining unit
520: steam coil 530: transfer pump
600: steam coil 700: gas outlet
S1: raw material storage part S2: steam supply part
S3: Sulfuric acid storage part S4: Reaction part
S5: Purification section S6: Final storage section

Claims (9)

(C) and then stored in a total of three storage tanks (100) for 84 hours to 88 hours after transporting waste liquid cooking oil and vegetable oil residues generated from the vegetable edible oil preservation processing company using a transportation vehicle (C) A raw material storage unit S1,
A steam supply unit S2 for supplying steam at 90 DEG C generated through the steam boiler 200 to mix with the raw material discharged from the raw material storage unit S1,
A sulfuric acid storage unit S3 for supplying 98% sulfuric acid stored in the sulfuric acid storage tank 300 by using an injection pump 310 for mixing with the raw material discharged from the raw material storage unit S1,
The raw material discharged from the raw material storage part S1, the steam heat supplied from the steam supply part S2 and the sulfuric acid supplied from the sulfuric acid storage part S3 are supplied to the agitator 410 provided in the reaction tank 400 for 8 hours A reaction part S4 for separating the upper part of the sludge into the fatty acid, the middle part of the sludge, and the lower part of the sludge into the waste water,
A refining unit S5 including a first refining unit 500 for refining the separated fatty acid and a second refining unit 510 for refining the refined fatty acid in the first refining unit 500;
And a final storage unit (S6) for storing the purified fatty acid through the purification unit (S5).
The method according to claim 1,
In each of the storage tanks 100, an inlet valve 103 is provided in a sub-pipe 102 for storing a raw material flowing through a main pipe 101 at an upper center, And a discharge pipe (105) for discharging the waste oil by opening and closing the discharge valve (104) for discharging the waste oil.
The method according to claim 1,
In order to discharge the fatty acid formed in the upper layer, the fatty acid discharge valve 401 is disposed in the reaction tank 400 to separate the upper layer, the middle layer and the lower layer by the stirrer 410. In order to discharge the sludge formed in the middle layer, A waste water discharge valve 403 for discharging wastewater is formed in the lower portion of the waste water discharge valve 401. The fatty acid discharged through the fatty acid discharge valve 401 is transferred to the refining portion S5, 402) is sent to the concentration tank of the wastewater treatment plant and the wastewater discharged to the wastewater discharge valve (403) is discharged to the wastewater treatment plant.
The method according to claim 1,
Wherein an ejector (210) is provided at a position where the raw material discharged from the raw material storage unit (S1) and the steam supplied from the steam supply unit (S2) are mixed with each other.
The method according to claim 1,
And a static mixer 320 for mixing the raw material discharged from the raw material storage unit S1 with steam supplied from the steam supply unit S2 and sulfuric acid supplied from the sulfuric acid storage unit S3, A fatty acid production apparatus using waste cooking oil.
The method according to claim 1,
A steam coil 520 is kept inside the first and second purification units 500 and 510 to maintain the temperature of 45 ° C. Each of the cells is refined for 8 hours. After the purification, the fatty acid activity is formed, And is transferred to the final storage section S6 by the transfer pump 530 provided outside the second purification section 510. The apparatus for producing fatty acid according to claim 1,
The method according to claim 1,
And a steam coil (600) for maintaining a temperature of 45 ° C is provided inside the final storage part (S6).
The method according to claim 1,
Wherein a gas outlet port (700) is provided in each of the raw material storage section (S1), the sulfuric acid storage section (S3), the reaction section (S4), the purification section (S5), and the final storage section (S6) .
5. The method of claim 4,
The ejector 210 has a cylindrical shape with a main hole 211 formed at an inner center thereof and a plurality of partitions 212 formed at an outer periphery of the main hole 211 to form a sub hole 213, 213) is provided integrally with the induction plate (214) for accelerating the flow velocity.

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