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WO2017078225A1 - Appareil de récupération de bio-huile faisant appel à un vent de plasma - Google Patents

Appareil de récupération de bio-huile faisant appel à un vent de plasma Download PDF

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Publication number
WO2017078225A1
WO2017078225A1 PCT/KR2016/002273 KR2016002273W WO2017078225A1 WO 2017078225 A1 WO2017078225 A1 WO 2017078225A1 KR 2016002273 W KR2016002273 W KR 2016002273W WO 2017078225 A1 WO2017078225 A1 WO 2017078225A1
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WO
WIPO (PCT)
Prior art keywords
hot air
unit
exhaust gas
reactor
plasma
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/KR2016/002273
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English (en)
Korean (ko)
Inventor
이병호
황리호
박상훈
최문규
곽민호
박기만
윤영민
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
DAEKYUNG ESCO Co Ltd
Vitzrotech Co Ltd
Original Assignee
DAEKYUNG ESCO Co Ltd
Vitzrotech Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by DAEKYUNG ESCO Co Ltd, Vitzrotech Co Ltd filed Critical DAEKYUNG ESCO Co Ltd
Publication of WO2017078225A1 publication Critical patent/WO2017078225A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/02—Plant or installations having external electricity supply
    • B03C3/04—Plant or installations having external electricity supply dry type
    • B03C3/14—Plant or installations having external electricity supply dry type characterised by the additional use of mechanical effects, e.g. gravity
    • B03C3/15—Centrifugal forces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • 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
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • 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
    • 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
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a bio-oil recovery apparatus using plasma hot air, and more particularly, to a bio-oil recovery apparatus using plasma hot air for recovering bio oil through pyrolysis using plasma hot air by introducing organic waste into a reactor. .
  • RPF Refuse Plastic Fuel
  • RDF Refuse Derived Fuel
  • Korean Patent No. 10-1376737 discloses a bio-oil production apparatus and a bio-oil production process using the same.
  • a bio oil is supplied through a reactor for receiving biomass from a silo, a cyclone for receiving a synthesis gas discharged from the reactor and then performing a separation process, and cooling the synthesis gas that is separated from the cyclone in the cyclone.
  • a non-condensing gas storage unit for separating and storing the non-condensing gas discharged from the condensation unit in stages, wherein the non-condensing gas stored in the non-condensing gas supply unit can be supplied to the reactor again. It is configured to be.
  • high temperature hot air of about 450 ° C. to 550 ° C. needs to be continuously supplied to the reactor as a pyrolysis reaction gas. Since the exhaust gas is used as a pyrolysis reaction gas, the combustion air injected when the oil or the gas is combusted is subjected to the combustion reaction, and the surplus oxygen remaining in the reactor is supplied to the reactor so that the oxygen concentration in the reactor gradually increases during continuous operation.
  • the oxygen remaining in the reactor is combined with the carbon constituting the organic waste is converted into carbon dioxide gas has a problem that the production of the bio-oil rapidly decreases as the operating time is longer.
  • the biooil recovered from the reactants produced by rapid pyrolysis of organic wastes has a higher viscosity than ordinary oils and is easily cured at room temperature so that they do not flow down as they stick to the inner surface of the reactor and the inner surface of the cyclone. Not only does the phenomenon occur frequently and the recovery rate drops, as well as a problem that takes a long time to clean the oil stuck to the inner surface of the reactor and the inner surface of the cyclone.
  • the biofuel particles in the vapor state are cooled and condensed by the oil sprayed from the condensation recovery facility installed at the rear of the reactor, but the fine oil bioparticles of fine mist particles are recovered. Since it is recycled through the exhaust gas circulation duct with the exhaust gas without condensation, there is also a problem that the oil is stuck to the exhaust gas circulation duct and the blower blade, which is an important cause of mechanical failure.
  • An object of the present invention for solving the problems according to the prior art is to thermally decompose using the plasma hot air generated by a plasma hot air fan in which the pyrolysis reaction gas is supplied only to nitrogen air, so that oxygen supply is essentially blocked in the entire system. Therefore, even if the operation time is long, the production of bio oil is not reduced and stable operation can be continued.
  • the reactor, the cyclone, and the electrostatic precipitator are formed in a double partition structure, and thermal hot air is supplied between the double partition walls. Therefore, as the whole wall is kept warm, bio-oil using plasma hot air can increase the recovery efficiency and lengthen the cleaning cycle by preventing the high viscosity bio oil from sticking to the inner wall of the reactor, cyclone and electrostatic precipitator. In providing a recovery device.
  • Bio oil recovery apparatus of the present invention for solving the above technical problem, pyrolysis unit for pyrolyzing the organic waste received by using the plasma hot air; An oil recovery unit for separating and cooling the biooil contained in the exhaust gas discharged from the pyrolysis unit to recover the oil; A gas circulation unit configured to circulate the exhaust gas discharged from the oil recovery unit to the pyrolysis unit; And an insulating hot wind supply unit for supplying thermal hot air for insulating the inside of the pyrolysis unit or the gas circulation unit.
  • the pyrolysis unit the reactor for supplying the organic waste to discharge the pyrolyzed exhaust gas to the oil recovery unit; And a plasma hot air fan for supplying the mixed hot air to the inside of the reactor by mixing the plasma hot air and the exhaust gas supplied from the gas circulation unit.
  • the reactor is formed of a double partition structure
  • the heat insulating hot air supply unit may supply the hot air for keeping warm between the double partition walls of the reactor to keep the interior of the reactor.
  • the inner bottom of the reactor may be provided with a plurality of flow nozzles or porous plates connected to the plasma hot air, and the mixed hot air may be supplied into the reactor through the plurality of flow nozzles or the porous plates.
  • the plasma hot air may be generated by using nitrogen gas as a carrier gas.
  • the hot air in which the plasma hot air and the exhaust gas supplied from the gas circulation unit are mixed may be 450 ° C to 550 ° C.
  • the oil recovery unit a cyclone for performing a separation process after receiving the exhaust gas discharged from the pyrolysis unit;
  • a cooling condenser connected to a rear end of the cyclone to recover bio-oil through cooling and condensing the exhaust gas which is separated from the fan in the cyclone;
  • an electrostatic precipitator connected to the rear end of the cooling condenser to recover the biooil on the fine particles not recovered from the cooling condenser by an electrostatic precipitating method.
  • the heat insulating hot air supply unit may supply the hot air for insulating between the double partition of the cyclone and the electrostatic precipitator to insulate the interior of the cyclone and the electrostatic precipitator .
  • the electrostatic precipitator may be configured such that one or two or more of the electrostatic precipitators are connected in series using either a flat electrostatic precipitator or a cylindrical electrostatic precipitator.
  • the gas circulation unit the storage tank for storing the exhaust gas discharged from the oil recovery unit; It may be configured to include; and a blower for supplying the exhaust gas stored in the reservoir to the pyrolysis unit.
  • the thermal insulation hot air supply unit a combustion burner for generating thermal insulation; It may be configured to include; and a blower for blowing and supplying the heat of insulation.
  • the high-temperature plasma hot air generated by using nitrogen as a carrier air in a plasma torch at the bottom of the reactor after inputting organic waste such as sawdust, palm oil residues, grasses, agricultural residues into the reactor as a pyrolysis reaction gas has the advantage of stable recovery of char and bio oil, which are economical, from the reactants generated by thermal decomposition of carbon components among the various components constituting the organic waste by supplying through cooling, collecting, and recycling.
  • the pyrolysis reaction gas is pyrolyzed using the plasma hot air generated by the plasma hot air supplied only with nitrogen air, so that the oxygen supply is fundamentally blocked in the entire system, so that the production amount of bio oil does not decrease even if the operation time is long. There is an advantage that stable operation can be continued without.
  • the reactor, the cyclone, the electrostatic precipitator is formed in a double partition structure, and as the hot air for thermal insulation is supplied between the double partition walls, the biooil with high viscosity is maintained in the reactor, cyclone, electrostatic precipitator. It is advantageous to increase the recovery efficiency and lengthen the cleaning cycle by suppressing the adhesion to the inner wall.
  • FIG. 1 is a block diagram showing the overall connection between the components of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.
  • FIG. 2 is a block diagram illustrating a pyrolysis unit of a biooil recovery apparatus using plasma hot air according to an embodiment of the present invention.
  • FIG. 3 is a block diagram showing an oil recovery unit of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.
  • Figure 4 is a block diagram showing a gas circulation unit of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.
  • FIG. 5 is a block diagram showing a heat insulation hot wind supply unit of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention.
  • fluid carrier storage tank 107 fluid carrier
  • Oil recovery part 201 Cyclone
  • cooling condenser 203 spray nozzle
  • electrostatic precipitator 300 gas circulation unit
  • the terms are used only for the purpose of distinguishing one component from another.
  • the first component may be referred to as the second component, and similarly, the second component may also be referred to as the first component.
  • FIG. 1 is a block diagram showing the overall connection relationship between the components of the bio-oil recovery apparatus using the plasma hot air according to an embodiment of the present invention
  • Figure 2 is a bio-oil using plasma hot air according to an embodiment of the present invention
  • 3 is a block diagram illustrating a pyrolysis unit of a recovery device
  • FIG. 3 is a block diagram showing an oil recovery unit of a biooil recovery device using plasma hot air according to an embodiment of the present invention
  • FIG. 4 is an embodiment of the present invention.
  • FIG. 5 is a diagram illustrating a gas circulation unit of a biooil recovery apparatus using plasma hot air
  • FIG. 5 is a diagram illustrating a heat insulation hot wind supply unit of a biooil recovery apparatus using plasma hot air according to an embodiment of the present invention.
  • Bio oil recovery apparatus using a plasma hot air as shown in Figure 1, the thermal decomposition unit 100, oil recovery unit 200, gas circulation unit 300 and thermal insulation hot air supply unit ( 400).
  • the pyrolysis unit 100 is a component that thermally decomposes the organic waste received using plasma hot air.
  • the oil recovery unit 200 is a component for separating and cooling the biooil contained in the exhaust gas discharged from the pyrolysis unit 100 and recovering the oil.
  • the gas circulation unit 300 is a component that circulates the exhaust gas discharged from the oil recovery unit 200 to the pyrolysis unit 100.
  • the heat insulation hot air supply unit 400 is a portion for supplying heat insulation for warming the inside of the thermal decomposition unit 100 or the gas circulation unit 300.
  • thermal decomposition unit 100 First, the thermal decomposition unit 100 will be described.
  • the pyrolysis unit 100 includes a reactor 101 and a plasma hot air blower 108.
  • the reactor 101 is a component for supplying the organic waste and exhausting the pyrolyzed exhaust gas to the oil recovery part 200.
  • the outer wall is formed in a double wall structure and has a cylindrical body 102 arranged vertically. It is configured to include.
  • the thermal hot air supplied from the thermal hot air supply unit 400 is supplied between the double wall structures, and the inside of the reactor 101 may be warmed by the thermal hot air, and thus, the reactor 101 ) It is possible to prevent the biooil having a high viscosity from adhering to and sticking to the inner inner wall.
  • the main body 102 of the reactor 101 has a heat insulating hot air inlet 112 formed at one point of the outer wall of the double wall structure, and the heat insulating hot air outlet 113 is formed at another point of the outer wall of the double wall structure.
  • the wall temperature of the reactor 101 is maintained at an average of 300 ° C. by the hot air of about 150 ° C. to 400 ° C. supplied from the heat insulating hot air supply unit 400.
  • a hot air supplied from the plasma hot air blower 108 is connected to the inside of the reactor 101 at the bottom of the inner bottom of the main body 102 forming the overall shape of the reactor 101.
  • a plurality of flow nozzles 103 for supplying are provided, and a supply port 109 connected to the plasma hot air fan 108 is formed below the main body 102, and hot air supplied through the supply port 109 is provided.
  • Hot air may be uniformly supplied through the plurality of flow nozzles 103. In order to supply the hot air evenly, the plurality of flow nozzles 103 may be replaced to allow hot air to be injected through the porous plate through the porous plate.
  • a raw material input conveyor 104 for dumping organic waste is installed on one side of the main body 102 so that the organic waste supplied through the raw material input conveyor 104 is supplied into the reactor 101.
  • the raw material injection hole 105 is formed.
  • a flow yarn inlet 107 for supplying the flow yarn supplied from the flow yarn storage tank 106 to the inside of the reactor 101 is formed at the other side of the center portion of the body 102, and The other side of the lower side is formed with a flow yarn discharge port 110 for discharging the supplied flow yarn, the rear end of the flow yarn discharge port 110 is connected conveyor 111 for transferring the discharged flow yarn to the flow yarn storage tank 106 Is installed.
  • the plasma hot air blower 108 mixes the plasma hot air generated by itself and the exhaust gas supplied from the gas circulation unit 300 to mix the hot air mixed into the reactor 101 (plasma hot air and exhaust gas are mixed. Hot air).
  • the plasma hot air blower 108 is formed in a rocket shape, the plasma torch 114 is provided at the inlet portion (left side of FIG. 2), the exhaust gas circulation duct 115 is connected to the middle portion thereof, and the outlet portion ( 2 is connected to the supply port 109.
  • the plasma torch 114 is composed of a cathode 116 and an anode 117, and when a high current of DC is applied between the cathode 116 and the anode 117 between the cathode 116 and the anode 117 Plasma flame is generated in this case, and when nitrogen, which is a reaction gas, is blown into the plasma torch 114, a nitrogen-based ultra high temperature plasma flame of about 1200 ° C. to 1500 ° C. is generated.
  • the temperature of the reaction gas suitable for supplying the reactor 101 is about 500 ° C., it is mixed with the low temperature circulating exhaust gas supplied from the exhaust gas circulation duct 115 inside the plasma hot air fan 108 to 450 ° C. A reaction gas in the range of 550 ° C. is generated and supplied to the reactor 101.
  • thermal decomposition unit 100 As described above, it is possible to thermally decompose organic waste such as sawdust, palm oil residues, grasses, agricultural residues, etc. supplied into the main body 102 of the reactor 101.
  • the oil recovery unit 200 includes a cyclone 201, a cooling condenser 202, and an electrostatic precipitator 204.
  • the cyclone 201 is a component for recovering char by separating the particulate matter by centrifugal force after accommodating the exhaust gas that is pyrolyzed and discharged from the pyrolysis unit 100, and has an outer wall having a double wall structure.
  • the inside of the reactor 101 by the warm hot air can be kept warm, Therefore, it is possible to prevent the biooil having a high viscosity from adhering to and sticking to the inner wall of the reactor 101.
  • an inlet for insulated hot air and an outlet for insulated hot air flow are formed at one point and another point of the outer wall of the double wall structure of the cyclone 201, respectively, and are supplied from the hot air supply unit 400.
  • the hot air of about 150 °C to 400 °C to maintain the wall temperature of the cyclone 201 can be an average of 300 °C.
  • Centrifuged ⁇ is collected and collected at the center lower portion of the cyclone 201, and exhaust gas containing bio-oil is supplied to the cooling condenser 202 through the upper portion of the cyclone 201.
  • the cooling condenser 202 is connected to a rear end of the cyclone 201 to recover bio-oil through cooling and condensation of the exhaust gas that is separably treated from the cyclone 201 and cooling condensation.
  • the bio oil is recovered through.
  • the cooling condenser 202 may be configured such that one or two or more are connected in series, and the biooil condensed through the cooling condenser 202 is stored in a separate oil storage tank (not shown). Can be.
  • the condensation of the biooil in the cooling condenser 202 may be achieved by spraying the bio-oil recovered in the oil storage tank through the injection nozzle 203 installed on the cooling condenser 202, the initial operation Since there is no biooil recovered from the cooling condenser 202, it is preferable to use paraffin oil or oil similar in physical properties to biocondensate as the condensate until the biooil is recovered to a certain amount.
  • the electrostatic precipitator 204 is connected to the rear end of the cooling condenser 202 to recover the biooil on the fine particles that are not recovered from the cooling condenser 202, to recover the biooil through the electrostatic precipitating method do.
  • Bio-oil contained in the gas is almost collected in the cooling condenser 202, but in the exhaust gas discharged from the cooling condenser 202, the bio-oil on the microparticles, which are not condensed and fly again, remain.
  • One or two or more units are provided in series at the rear end of the cooling condenser 202 to collect oil.
  • the outer wall of the electrostatic precipitator 204 is formed of a double partition wall structure
  • the heat insulating hot air supply unit 400 supplies the hot air for insulating between the double partition walls of the electrostatic precipitator 204 to the electrostatic precipitator 204 It is configured to insulate the interior of the.
  • an inlet for insulated hot air and an outlet for inflowing the warmed hot air are formed at one point and the other point of the outer wall of the double partition wall structure of the electrostatic precipitator 204, respectively.
  • the hot air supplied from about 150 ° C. to 400 ° C. maintains the wall temperature of the cyclone 201 to be 300 ° C. on average.
  • the electrostatic precipitator 204 may be any one of a flat plate-type electrostatic precipitator having a flat plate or a cylindrical electrostatic precipitator having a cylindrical plate, but to increase the mist collecting efficiency of the droplet state contained in the exhaust gas, a cylindrical electrostatic precipitator. It is preferable to use a flat type electrostatic precipitator for stable operation, and it is preferable to configure the cylindrical electrostatic precipitator and the flat type electrostatic precipitator in order to achieve both mist collection efficiency and stable operation.
  • the oil recovery unit 200 As described above, it is possible to recover the bio-oil contained in the exhaust gas supplied from the pyrolysis unit 100, in particular, fine contained in the exhaust gas through the electrostatic precipitator 204 Since the biooil on the particles is collected and recovered, the biooil microparticles are prevented from mechanical failure due to attachment and fixation inside the components, and the recovery rate of the biooil can be maximized.
  • the gas circulation unit 300 includes a reservoir 301 and a blower 302.
  • the storage tank 301 is a component for storing the exhaust gas discharged from the oil recovery unit 200, the blower 302 for supplying the exhaust gas stored in the storage tank 301 to the pyrolysis unit 100. Component.
  • the blower 302 allows the exhaust gas stored in the reservoir 301 to be supplied into the plasma hot air blower 108 through the circulation duct 115 connected to the middle portion of the plasma hot air blower 108.
  • the reservoir 301 and the exhaust gas circulation duct 115 is preferably configured in a closed structure, because the outside air is introduced into the exhaust gas while the oxygen is not included, and the organic waste is thermally decomposed Char and bio-oil are recovered from the generated reactants, but the remainder is gasified to be included in the exhaust gas, and if the operation continues, the amount of exhaust gas gradually increases, so that the gas vent valve 303 is attached to the upper portion of the exhaust gas storage tank 301. It is preferable to allow some of the exhaust gas to be discharged manually or automatically.
  • the bio-oil is recovered, and the low temperature exhaust gas is supplied back to the plasma hot air fan 108 so that the temperature of the plasma hot air can be properly adjusted.
  • thermal insulation hot air supply unit 400 Next, the thermal insulation hot air supply unit 400 will be described.
  • the warm hot air supply unit 400 as shown in Figure 5, comprises a combustion burner 401 and a blower 402.
  • the combustion burner 401 is a component that generates warm heat through combustion using LNG or oil as fuel
  • the blower 402 is a component that blows and supplies the warm heat.
  • blower 402 is blown so that hot air can be supplied through the inlet of the thermal hot air of the reactor 101, the cyclone 201, the electrostatic precipitator 204.
  • the wall temperature of the reactor 101, the cyclone 201, the electrostatic precipitator 204 can be maintained to be an average of 300 °C, through which the bio-oil It can flow along the inner wall of the to increase the collection efficiency, it is possible to increase the internal cleaning cycle of the recovery facility.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Physics & Mathematics (AREA)
  • Plasma & Fusion (AREA)

Abstract

La présente invention concerne un appareil de récupération de bio-huile faisant appel à un vent de plasma, l'appareil introduisant des déchets organiques dans un réacteur et récupérant la bio-huile au moyen d'une pyrolyse faisant appel à un vent de plasma. Pour ce faire, l'appareil de récupération de bio-huile faisant appel à un vent de plasma selon l'invention est conçu pour comprendre : une unité de pyrolyse qui utilise le vent de plasma et pyrolyse les déchets organiques reçus; une unité de récupération d'huile qui sépare, refroidit et récupère la bio-huile contenue dans le gaz d'échappement déchargé de l'unité de pyrolyse; une unité de circulation de gaz qui introduit le gaz d'échappement déchargé de l'unité de récupération d'huile dans l'unité de pyrolyse et fait circuler ledit gaz; et une unité d'alimentation en vent thermique qui insuffle un vent thermique pour maintenir la chaleur à l'intérieur de l'unité de pyrolyse ou de l'unité de circulation de gaz.
PCT/KR2016/002273 2015-11-06 2016-03-08 Appareil de récupération de bio-huile faisant appel à un vent de plasma Ceased WO2017078225A1 (fr)

Applications Claiming Priority (2)

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KR1020150155882A KR101831897B1 (ko) 2015-11-06 2015-11-06 플라즈마 열풍을 이용한 바이오오일 회수장치
KR10-2015-0155882 2015-11-06

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WO2017078225A1 true WO2017078225A1 (fr) 2017-05-11

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Cited By (5)

* Cited by examiner, † Cited by third party
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CN107413524A (zh) * 2017-08-03 2017-12-01 可迪尔空气技术（北京）有限公司 一种含石蜡油雾治理装置
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CN107413524B (zh) * 2017-08-03 2024-02-02 可迪尔空气技术（北京）有限公司 一种含石蜡油雾治理装置
CN108800151A (zh) * 2018-04-29 2018-11-13 江燕婷 一种绿色环保的工业垃圾焚烧炉
CN108800151B (zh) * 2018-04-29 2019-09-13 无锡方菱环保科技有限公司 一种绿色环保的工业垃圾焚烧炉
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