WO2019098556A1 - 바이오디젤 제조 장치 및 방법 - Google Patents
바이오디젤 제조 장치 및 방법 Download PDFInfo
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- WO2019098556A1 WO2019098556A1 PCT/KR2018/012677 KR2018012677W WO2019098556A1 WO 2019098556 A1 WO2019098556 A1 WO 2019098556A1 KR 2018012677 W KR2018012677 W KR 2018012677W WO 2019098556 A1 WO2019098556 A1 WO 2019098556A1
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- Prior art keywords
- catalyst
- biodiesel
- alcohol
- oil
- hours
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the present invention relates to an apparatus and a method for manufacturing biodiesel, and more particularly, to an apparatus and a method for manufacturing biodiesel using biodiesel including vegetable oil or animal oil including waste cooking oil.
- Fossil fuels such as petroleum and coal, which are currently being used as energy sources, are not only depletion resources with limited reserves but also environmental pollution problems such as carbon dioxide generation. Therefore, alternative energy sources that can replace fossil fuels have been studied in a variety of ways, one of which is biodiesel that can be produced from vegetable or animal fats.
- Patent Publication No. 10-0746219 discloses an apparatus for producing biodiesel by mixing vegetable oil with sodium hydroxide and methanol. In order to uniformly mix vegetable oil with sodium hydroxide and methanol, And a stirring blade is used.
- the present invention has been made in order to solve the problems of the prior art, and it is an object of the present invention to provide an apparatus and a method for manufacturing biodiesel, in which production time is greatly reduced as well as productivity of a manufacturing facility is reduced.
- Another object of the present invention is to provide an apparatus and a method for producing biodiesel capable of producing biodiesel during all seasons irrespective of the season and improved productivity.
- an apparatus for manufacturing biodiesel includes: a holding reservoir for storing a waste such as waste cooking oil; A catalyst processor supplied with the oil stored in the holding tank and pressurized and aerated in a state where the catalyst is supplied; And an alcohol reactor supplied with the feed transferred from the catalyst processor and pressurized and aerated in a state where the alcohol is supplied.
- the catalyst processor includes a treatment tank for containing the oil and the catalyst; And a first oxidation floatation device installed on the upper part of the treatment tank and pressurized and aerated in the treatment tank.
- the catalyst processor may further include a heater installed in a lower portion of the treatment tank to apply heat to the treatment tank.
- the alcohol reactor is a reaction tank for holding the oil and the alcohol;
- a second oxidative flotation device installed at the upper part of the reaction tank and pressurized and aerated in the reaction tank;
- a reaction tank heater provided at a lower portion of the reaction tank for applying heat to the reaction tank.
- the time period during which the first oxidation floater is pressurized and aerated is in the range of 1 hour to 2 hours
- the time period during which the second oxidation floater is pressurized and aerated in the alcohol reaction tank is in the range of 2 hours to 3 hours
- the time for stabilization after the operation of the second oxidation floater is stopped is in the range of 1 hour to 2 hours.
- the alcohol reactors include a biodiesel discharge pipe having one end thereof installed in the reaction tank and discharging the produced biodiesel; And an interface sensor formed at one end of the biodiesel discharge pipe, so that biodiesel and glycerin can be separated. Further, it may further comprise an air injector injecting air from the lower part of the reaction tank to promote the esterification reaction.
- a filter disposed between the holding tank and the catalyst processor may be installed and filtered.
- the method of manufacturing biodiesel includes: a catalyst pretreatment step of supplying a catalyst to a fuel oil and pressurizing and aeration; An alcohol reaction step of supplying alcohol to the oil after the catalyst pretreatment step and pressurizing and aeration; And then a pressurization aeration is stopped and the resulting glycerin and biodiesel are separated by the specific gravity difference.
- the reaction in the alcohol reaction step and the stabilization step, the reaction can be promoted by heating to 50-70 ° C.
- the catalyst pre-treatment step is performed within a range of 1 hour to 2 hours
- the alcohol reaction step is performed within a range of 2 hours to 3 hours
- the stabilization step can be performed within a range of 1 hour to 2 hours .
- the apparatus for manufacturing biodiesel according to an embodiment of the present invention since the apparatus for manufacturing biodiesel according to an embodiment of the present invention has a relatively simple structure, the facility volume is greatly reduced.
- the method of manufacturing biodiesel according to one embodiment of the present invention is characterized in that the oil and the catalyst are first pressurized and aerated, uniformly mixed, and then the alcohol is pressurized and aerated to uniformly mix. The production time of the biodiesel can be greatly reduced and the biodiesel having a high octane number can be produced.
- biodiesel can be produced regardless of the season because it can be suitably heated in the catalyst pretreatment step or the alcohol reaction step, and biodiesel can be efficiently produced even when the viscosity of waste cooking oil is high.
- productivity can be further improved because biodiesel and glycerin can be effectively separated.
- FIG. 1 is a block diagram illustrating an apparatus for manufacturing biodiesel according to an embodiment of the present invention
- Fig. 2 is a view of the catalyst processor of Fig. 1,
- FIG. 3 is a view showing the alcohol reactor of FIG. 1,
- Fig. 4 is a view showing a part of the alcohol reactor of Fig. 1,
- FIG. 5 is a flowchart of a method for manufacturing biodiesel according to an embodiment of the present invention.
- the apparatus for manufacturing biodiesel according to an embodiment of the present invention includes a waste cooking oil storage tank 100, a filter 200, a catalyst processor 300, an alcohol reactor 400, a glycerine storage tank 500, and a biodiesel storage tank 600 ).
- biodiesel is produced by regenerating waste cooking oil.
- waste cooking oil is merely an example.
- the present invention can be applied not only to waste cooking oil but also various vegetable or animal oils as raw materials for biodiesel, Or the new oil before use may be used.
- the waste cooking oil storage tank 100 is a storage tank for storing waste cooking oil used for deep-fried cooking or the like, and is connected to the filter 200.
- the filter 200 is composed of one or a plurality of membrane filters, and primarily filters waste of waste cooking oil.
- the waste cooking oil having relatively good condition can be used as regenerating cooking oil again through the filter 200.
- Such regenerating cooking oil is stored in the regenerating cooking oil reservoir 700 after passing through the filter 200.
- the filter 200 and the like are provided to explain the regeneration of the waste cooking oil.
- fresh oil that is, unused vegetable or animal oil is used as the raw material of the biodiesel, Can be omitted.
- the catalytic processor 300 is a device in which the oil filtered in the filter 200 is pretreated by a catalyst, and its configuration is shown in Fig.
- the catalyst processor 300 includes a supply pipe 311, a treatment tank 310, a first oxidation floating device 320, a heater 330, a catalyst storage 390, a catalyst supply pipe 391, And a discharge pipe 350 through which the refrigerant is discharged.
- the oil that has passed through the filter 200 is supplied to the treatment tank 310 by the pump P23 and the catalyst is supplied through the catalyst supply pipe 391 in the catalyst storage unit 390, Is provided by the catalyst.
- the catalyst may be a basic catalyst such as sodium hydroxide or an acidic catalyst.
- the catalyst may be in a liquid state or a solid state, and a natural or synthetic catalyst may be used. Further, the supply of the catalyst may be manually supplied by a required amount, and may be connected to a controller (not shown) to automatically supply the required amount.
- the first oxidation flotation device 320 is installed in the treatment tank 310 and is configured to pressurize the oil and the carrier.
- the first oxidation floater 320 is pressurized and aerated to a predetermined pressure, that is, 20 kgf / cm 2 .
- the first oxidizing floatator 320 rotates the impeller 324 connected to the shaft 323 by driving the motor 321 so that the first oxidizing floater 320 can flow in from the outside through the air inflow pipe 322 disposed around the impeller 324,
- the air in the treatment tank 310 is injected into the mixed mixture, and the injected air causes the catalyst and the oil to be uniformly mixed and agitated.
- the air inlet pipe 322 may be disposed around the impeller 324 at equal intervals of 12 to 24.
- the plurality of air inflow pipes 322 uniformly inflow air in the circumferential direction and aeration to the oil in accordance with the rotation of the impeller 324.
- the spirally rotating air bubbles can uniformly mix the oil and the catalyst evenly, and the treatment time can be greatly reduced.
- the catalytic processor 300 may also include a first heater 330 for properly heating to lower the viscosity of the oil when the viscosity of the oil is high.
- a first heater 330 for properly heating to lower the viscosity of the oil when the viscosity of the oil is high.
- the oil may be heated by appropriately heating the oil with the first heater 330 and used.
- the catalyst processor 300 includes a temperature sensor (not shown) in the treatment tank 310 to connect the temperature sensor to the controller, and controls the first heater 330 of the treatment tank 310 can do.
- the processor 300 may include a viscosity sensor not shown in the treatment bath 310 to control the first heater 330 of the treatment bath 310 based on the sensed viscosity.
- An upper opening / closing port 360 may be provided at the upper end of the treatment tank 310 as needed to remove the vapor and the generated gas.
- the oil mixed with the catalyst in the catalyst processor 300 is agitated for 2-3 hours by being pressurized and aerated by the first oxidation floater 320, and thus the total production time can be greatly reduced.
- the discharge pipe 350 discharges the oil pretreated by the catalyst to the alcohol reactor 400 by the pump P34.
- the alcohol reactor 400 is a device for separating the glycerin and diesel flow path by increasing the octane number of the diesel oil by reacting the oil pretreated by the catalyst with alcohol, and FIG. 3 shows the structure thereof.
- the alcohol reactor 400 supplies alcohol to the reaction tank 410 through a supply pipe 411, a reaction tank 410, an alcohol storage unit 490 and an alcohol storage unit 490 for supplying the oil discharged from the treatment tank 310
- a second oxidizing flotation device 420 for pressurizing and aeration the oil reacting with the alcohol, a second heater 430, an air injector 440 for aeration in the oil-reactive oil,
- a pump P45 for discharging glycerin into the glycerin storage tank 500 and a glycerin discharge pipe 460 and a pump P46 for discharging the generated biodiesel to the biodiesel storage tank 600 and a biodiesel discharge pipe 460 .
- the reaction tank 410 provides a space for accommodating the supplied catalytically-treated fat to react with the alcohol. That is, in the reaction tank 410, the alcohol is supplied through the alcohol supply pipe 491 in the alcohol storage unit 490 to provide a space where the oil and the alcohol react. At this time, the alcohol may be a lower alcohol such as methanol. In addition, the alcohol can be supplied manually by the required amount, and can be connected to a controller (not shown) to automatically supply the required amount.
- the alcohol reactor 400 includes a second oxidizer float 420 and a second heater 430 to uniformly react the alcohol and the oil and to evaporate water.
- the second oxidation floater 420 and the second heater 430 are shown as two in FIG. 3, the second oxidation floater and the second heater may be installed in one or more appropriate number .
- the construction of the second oxidation floater 420 is the same as that of the first oxidation floater 320. That is, the second oxidation floater 420 is installed in the reaction tank 410 to pressurize the oil reacting with the alcohol.
- the second oxidizer float 420 is pressurized and aerated to a predetermined pressure, approximately 20 kgf / cm 2 .
- the oxidizer flotator 420 rotates the impeller 424 connected to the shaft 423 by driving the motor 421 so that the air flowed from the outside through the air inlet pipe 422 disposed around the impeller 424 Is injected into the mixed fuel of the catalyst in the reaction tank 410, and the injected air causes the catalyst and the oil to be uniformly mixed and agitated.
- the air inlet pipe 422 may be disposed around the impeller 424 at equal intervals of 12 to 24.
- the plurality of air inflow pipes 422 uniformly inflow air in the circumferential direction and aeration to the oil as the impeller 424 rotates.
- the catalyst-treated oil and the alcohol are pressurized and aerated by the second oxidizing floatation device 420 to promote the reaction by uniformly mixing the alcohol and the oil by the spirally rotating air bubbles. That is, in the case of mixing the catalyzed oil with the alcohol by pressurization aeration by the oxidative flotation device as in the present invention, the air bubbles can be mixed with the alcohol uniformly so that the esterification reaction time can be greatly reduced. That is, the oil reacts with the alcohol in the presence of the catalyst to produce esterified oil and glycerin. Further, when the alcohol is mixed later with the catalyst and the alcohol, the octane number of the produced biodiesel becomes higher.
- a separate air injector 440 may be installed at the lower end of the reaction vessel 410 to further accelerate water evaporation.
- the air injector 440 has a cylindrical shape and a fine air outlet formed therein to discharge air to accelerate the evaporation of water.
- an upper opening / closing port (not shown) may be provided as needed to remove the vapor and water.
- the oil reacted with the alcohol in the reaction tank 410 is pressurized and aerated by the second oxidation floater 420 and stirred for 2-3 hours to produce biodiesel having a high octane number.
- the stabilization time of 1-2 hours is elapsed in order to stop the operation of the second oxidation floater 420 and to separate the glycerin and the biodiesel. Due to the difference in the specific gravity of biodiesel and glycerin produced after the stabilization time, Will sink downward and biodiesel will float upwards.
- the difference in specific gravity between glycerin and biodiesel is used to separate glycerin and biodiesel. That is, in order to separate the lowered glycerin into the glycerin storage tank 500, the glycerin discharge pipe 460 discharges the glycerin from the lower side of the treatment tank 410 by the pump P45. The discharged glycerin is stored in the glycerin storage tank 500 through the glycerin transfer pipe 511.
- the biodiesel discharge pipe 460 is disposed above the treatment tank 410 to discharge the biodiesel by the pump P46, and the discharged biodiesel is discharged from the biodiesel transfer pipe And stored in the biodiesel storage tank 600 through the pipe 611.
- a glycerin adsorption filter (not shown) may be installed in the biodiesel transfer pipe 611 to separate the biodiesel having higher purity.
- FIG. 4 is a view for explaining a method of separating biodiesel using an interface sensor 470 for sensing an interface (I) between biodiesel and glycerin.
- the interface sensor 470 an optical molecular sensor or an ultrasonic sensor can be used. That is, when the biodiesel and the glycerin are separated in the stabilization step, the biodiesel discharge pipe 460 discharges the biodiesel present in the upper part of the reaction tank 410, and the interface sensor 470 continuously detects the interface. If the interface (I) is not detected, the biodiesel emission is continued, and when the interface (I) is detected, the biodiesel emission is stopped.
- the actuator 480 is connected to move the interface sensor 470 and the biodiesel discharge pipe 460 up and down so that the end of the interface sensor 470 and the biodiesel discharge pipe 460 are moved from the upper side to the lower side, It is possible to discharge the biodiesel while detecting. After the biodiesel is completely drained, the pump (P45) can be operated to discharge the glycerin.
- Fig. 5 shows a flow chart of this manufacturing method.
- the waste cooking oil used for deep-fried cooking or the like is stored in the waste cooking oil storage tank 100 (step S10), and the waste cooking oil is filtered through the filter 200.
- the oil that has passed through the filter 200 is stored in the regeneration oil storage tank 700 of Fig. 1 if it can be regenerated as cooking oil.
- Step S30 As described above, unused vegetable or animal fat is used as a raw material , It can be supplied directly to the catalyst processor 300 in the storage tank.
- the first oxidizing flotation device 320 promotes the separation of the oil from the glycerin and the diesel oil by pre-treating the airborne air generated by pressurization and aeration by uniformly mixing the oil and the catalyst. At this time, if the first oxidation floater 320 can be pressurized and aerated at a predetermined pressure, the set pressure is approximately 20 kgf / cm 2 . The oil is pressurized and aerated in the catalyst processor 300 in the presence of the catalyst for about 1-2 hours.
- the viscosity of the oil retainer when the viscosity of the oil retainer is high even in the winter season or the summer season, the viscosity of the oil retainer can be lowered by operating the first heater 330 to lower the viscosity of the oil retainer.
- Step S40 Specifically, the maintenance is transferred into the reaction tank 410 of the alcohol reactor 400, and the alcohol stored in the alcohol storage portion 490 is supplied manually or automatically through the alcohol supply pipe 491.
- the second oxidation floater 420 is operated to pressurize and aeration, and the air bubbles generated at this time promote the reaction between the oil and the alcohol by uniform mixing. At this time, if the second oxidizing float 420 can be pressurized and aerated at the set pressure, the set pressure is approximately 20 kgf / cm 2 .
- the moisture contained in the oil can be moved upward in the oil retainer to accelerate the evaporation of water .
- the air injector 440 may be operated at the lower end of the reaction tank 410 to further accelerate the evaporation of moisture, thereby blowing air bubbles upward.
- the oil is pressurized a little with the alcohol in the alcohol reactor (400) for about 2-3 hours to increase the octane number of the diesel oil, and moisture can be removed.
- Step S50 In this stabilization step, due to the difference in specific gravity of biodiesel and glycerin, glycerin sinks downward and biodiesel floats upward, and biodiesel and glycerin are separated above and below the interface.
- the second heater 430 is preferably operated continuously.
- the separated biodiesel and glycerin are transferred to the biodiesel storage tank 600 and the glycerin storage tank 500, respectively, and stored.
- the interface sensor 470 can be used to discharge the biodiesel. While the biodiesel discharge pipe 460 is lowered from the upper side of the reaction tank 410 and the interface I is not detected, Diesel is discharged. That is, if the interface sensor 470 does not detect the interface I, the biodiesel discharge is continued, and when the interface I is detected, the biodiesel discharge is stopped.
- the glycerin can be discharged through the glycerin outlet pipe 450.
- the biodiesel exhaust pipe 460 and the biodiesel storage tank 600 can be filtered using a glycerin adsorption filter.
- the apparatus for producing biodiesel of the present invention since the apparatus for producing biodiesel of the present invention has a relatively simple structure of a catalyst treatment tank and an alcohol reaction tank, the facility volume is greatly reduced. Further, in the present invention, since the oil and the catalyst are first pressurized and aerated and uniformly mixed, then the alcohol is pressurized and aerated and then mixed uniformly, so that the esterification reaction can be promoted, and the production time of the biodiesel can be greatly reduced A biodiesel having a high octane number can be produced.
- biodiesel can be produced regardless of the season because it can be suitably heated in the catalyst pretreatment step or the alcohol reaction step, and biodiesel can be efficiently produced even when the viscosity of waste cooking oil is high.
- the productivity can be further improved because the biodiesel and glycerin can be effectively separated relatively easily.
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- Organic Chemistry (AREA)
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- General Chemical & Material Sciences (AREA)
- Liquid Carbonaceous Fuels (AREA)
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Abstract
Description
Claims (11)
- 유지를 저장하는 유지 저장조;상기 유지 저장조에 저장된 유지가 공급되며, 촉매가 공급된 상태에서 가압 폭기하는 촉매 처리기; 및상기 촉매 처리기에서 이송된 유지가 공급되며, 알코올이 공급된 상태에서 가압 폭기하는 알코올 반응기;를 포함하고,상기 촉매 처리기는유지와 촉매를 수용하는 처리조; 및상기 처리조 내의 상부에 설치되어, 상기 처리조 내에 가압 폭기하는 제1 산화부상기를 포함하고,상기 알코올 반응기는유지와 알코올을 수용하는 반응조;상기 반응조 내의 상부에 설치되어, 상기 반응조 내에 가압 폭기하는 제2 산화부상기; 및상기 반응조 내의 하부에 설치되어, 상기 반응조 내에 열을 가하는 반응조 히터를 포함하는 바이오디젤 제조 장치.
- 제1항에 있어서,상기 촉매 처리기는 상기 처리조 내의 하부에 설치되어, 상기 처리조 내에 열을 가하는 처리조 히터를 더 포함하는 바이오디젤 제조 장치.
- 제1항에 있어서,상기 촉매 처리조에서 제1 산화부상기가 가압 폭기하는 시간이 1시간 내지 2시간의 범위인 바이오디젤 제조 장치.
- 제1항에 있어서,상기 알코올 반응조에서 제2 산화부상기가 가압 폭기하는 시간이 2시간 내지 3시간의 범위이고,제2 산화부상기의 동작이 정지된 후 안정화 상태의 시간이 1시간 내지 2시간의 범위인 바이오디젤 제조 장치.
- 제1항 또는 제4항에 있어서,상기 알코올 반응기는상기 반응조 내에 그 일단이 설치되어, 제조된 바이오디젤을 배출하는 바이오디젤 배출관; 및상기 바이오디젤 배출관의 일단에 형성된 계면 센서를 포함하는 바이오디젤 제조 장치.
- 제1항에 있어서,상기 알코올 반응기는 상기 반응조의 하부에서 공기를 주입하는 공기 주입기를 더 포함하는 바이오디젤 제조 장치.
- 제1항에 있어서,상기 유지 저장조와 상기 촉매 처리기 사이에 배치된 여과기를 더 포함하는 바이오디젤 제조 장치.
- 식물성 또는 동물성 유지를 사용하여 바이오디젤을 제조하는 방법으로서,유지에 촉매를 공급하고, 가압 폭기하는 촉매 전처리 단계;상기 촉매 전처리 단계를 거친 유지에 알코올을 공급하고, 가압 폭기하는 알코올 반응 단계;상기 가압 폭기를 정지하고 유지가 비중 차이에 의하여 글리세린과 바이오디젤로 분리되도록 하는 안정화 단계;를 포함하는 바이오디젤 제조 방법.
- 제8항에 있어서,상기 알코올 반응 단계와 안정화 단계에서, 50-70℃로 가열하는 것을 특징으로 하는 바이오디젤 제조 방법.
- 제8항에 있어서,상기 촉매 전처리 단계는 1시간 내지 2시간의 범위 내에서 수행되고,상기 알코올 반응 단계는 2시간 내지 3시간의 범위 내에서 수행되고,상기 안정화 단계는 1시간 내지 2시간의 범위 내에서 수행되는 바이오디젤 제조 방법.
- 제8항에 있어서,상기 촉매 전처리 단계에서 유지를 가열하는 것을 특징으로 하는 바이오디젤 제조 방법.
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KR100752592B1 (ko) * | 2007-02-13 | 2007-08-29 | 서강오씨아이 주식회사 | 폐수가 발생하지 않는 친환경 바이오 디젤유의 제조장치 및그 제조방법 |
KR100858663B1 (ko) * | 2008-02-12 | 2008-09-17 | 김재남 | 폐식용유를 이용한 바이오디젤의 제조장치 |
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KR100752592B1 (ko) * | 2007-02-13 | 2007-08-29 | 서강오씨아이 주식회사 | 폐수가 발생하지 않는 친환경 바이오 디젤유의 제조장치 및그 제조방법 |
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