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WO2015026023A1 - Réacteur de gazéification utilisant une biomasse - Google Patents

Réacteur de gazéification utilisant une biomasse Download PDF

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Publication number
WO2015026023A1
WO2015026023A1 PCT/KR2014/001057 KR2014001057W WO2015026023A1 WO 2015026023 A1 WO2015026023 A1 WO 2015026023A1 KR 2014001057 W KR2014001057 W KR 2014001057W WO 2015026023 A1 WO2015026023 A1 WO 2015026023A1
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WO
WIPO (PCT)
Prior art keywords
reactor
biomass
air
air supply
zone
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/KR2014/001057
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English (en)
Korean (ko)
Inventor
김종표
홍선일
손진국
이재구
홍성구
김명준
김의용
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.)
SAMYANG ECO-ENERGY Co Ltd
Original Assignee
SAMYANG ECO-ENERGY 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 SAMYANG ECO-ENERGY Co Ltd filed Critical SAMYANG ECO-ENERGY Co Ltd
Priority to CN201480000969.7A priority Critical patent/CN104640959B/zh
Publication of WO2015026023A1 publication Critical patent/WO2015026023A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

  • the present invention relates to a gasification reaction apparatus using biomass, and more particularly, to produce biomass in a solid state as a synthesis gas such as hydrogen, carbon monoxide, and methane in a gaseous state by thermal and chemical energy conversion.
  • the present invention relates to a gasification reaction apparatus using biomass to generate electric power by using a synthesis gas as a heat source of a boiler or a fuel of an internal combustion engine.
  • gasification is the production of solid materials in the form of syngas, which is a gaseous material by thermal and chemical energy conversion methods, and is mainly applied to coal, waste, woody biomass (rice husk, Corn stalks, sawdust, wood chips).
  • the gasification method is largely classified into a fixed bed method and a fluidized bed method, and the fixed bed method is subdivided into a bottom-up gasification method, a top-down gasification method, and a countercurrent gasification method, and the fluidized bed method is a circulating fluidized bed gasification method or a bubble bed fluidized bed gasification method. Can be divided.
  • the bottom-up gasification method is a method in which a solid raw material is input from the upper side and a gasification oxidant is supplied in a direction opposite to the solid raw material.
  • the solid material may be divided into a drying zone, a pyrolysis zone, a reduction zone, and an oxidation zone from a top side into which the solid raw material is introduced.
  • the air as an oxidant is mainly supplied from the lower side to the upper side into which the raw material is input, so that the heat transfer efficiency is good for the solid raw material to be introduced, and the outlet temperature is relatively low, such as 250 to 300 degrees Celsius. Due to its high tar content, it is mainly used as a heat source replacement technology for boilers.
  • the top-down gasification method is a system in which the input direction of the solid raw material and the input direction of air are parallel.
  • drying zone pyrolysis zone
  • pyrolysis zone pyrolysis zone
  • combustion zone reduction zone from the top of which solid raw material is input. It is the same direction as the input direction of the raw material.
  • the thermal efficiency is relatively low and only heat transfer by radiant heat results in the discharge of the synthesis gas.
  • the temperature is relatively high at 700 ⁇ 750 degrees Celsius.
  • the top-down gasification method has a relatively small amount of tar in the syngas (about 95 to 99% reduction in tar)
  • the syngas generated by the top-down gasification method can be directly injected into a generator of an internal combustion engine and used as fuel. It is enough, and it is a technology that allows cogeneration with heat and electricity.
  • the countercurrent gasification method can be said to be a mixture of a bottom-up gasification method and a top-down gasification method, and the oxidizing agent is introduced from the side, and the tar decomposition rate in the syngas is lowered, and a low-density solid such as chaff and sawdust is mainly used. It is suitable for gasifying raw materials.
  • the gasifier using the top-down gasification method has the same direction of injecting the solid raw material and the air as the oxidizing agent, and as a result, the heat transfer efficiency between the solid raw material and the air decreases, so that the sensible heat temperature of the syngas discharged is relatively high. Same as one.
  • the present invention has been invented to improve the above problems, and provides a gasification reaction apparatus using a biomass that can be selectively operated according to the nature and type of the biomass to be introduced and to increase the production of syngas. It is to.
  • the present invention is to provide a gasification reaction apparatus using a biomass to increase the energy efficiency by recovering the sensible heat of the syngas discharged to increase the temperature of the air supplied to the oxidant and put it back into the gasification process.
  • the present invention as a technical idea for solving the above object is to produce a synthesis gas (syngas) from the biomass by introducing a biomass (biomass) and air as an oxidant from the upper side, A reactor in which a drying zone, a pyrolysis zone, a combustion zone, and a reduction zone are sequentially formed from above; A plurality of first air supply assemblies disposed to be spaced apart along the outer surface of the reactor so as to penetrate downward from the upper side of the reactor and extend to the oxidation zone, and supply air for combustion of the biomass to the oxidation zone; Spaced apart along the outer surface of the reactor so as to penetrate downwardly from the top of the reactor to extend to the oxidation zone, and is disposed between the first air supply assembly and a neighboring first air supply assembly, and the combustion of the biomass A plurality of second air supply assemblies for supplying more air to the oxidation zone than the first air supply assembly, and a gas outlet formed at a lower side of the reactor, and the syngas discharged from the reduction zone;
  • the present invention has a first and second air supply assembly that can selectively adjust the air supply amount to the oxidation region according to the nature and type of the biomass to be injected, thereby applying a wide range of biomass of various types to high efficiency and high quality Syngas can be produced.
  • the present invention has a heat exchange unit that can reuse the high sensible heat of the syngas produced and discharged due to the structural characteristics of the top-down gasification method again to heat the air required for the gasification process, thereby minimizing unnecessary waste of energy and It is possible to improve the production efficiency.
  • FIG. 1 is a cross-sectional conceptual view showing the overall configuration of a gasification reaction apparatus using biomass according to an embodiment of the present invention.
  • Figure 2 is a plan view of the gasification reaction apparatus using a biomass according to an embodiment of the present invention.
  • FIG 3 is a cross-sectional conceptual view showing the overall configuration of a second air supply assembly which is a main part of a gasification reaction apparatus using biomass according to an embodiment of the present invention.
  • FIG. 1 is a cross-sectional conceptual view showing the overall configuration of a gasification reaction apparatus using a biomass according to an embodiment of the present invention
  • Figure 2 is a plan view conceptual diagram of a gasification reaction apparatus using a biomass according to an embodiment of the present invention
  • 3 is a cross-sectional conceptual view showing the overall configuration of a second air supply assembly which is a main part of a gasification reaction apparatus using biomass according to an embodiment of the present invention.
  • a transparent arrow in FIG. 1 indicates a moving direction of the syngas 105 discharged from the reduction region 104
  • an arrow indicated by a dashed-dotted line indicates a direction in which ash of the biomass 108 is discharged.
  • Arrows indicated by the dashed-dotted line indicate the moving direction of the coolant flowing into and exiting the cooling jacket 680.
  • arrows indicated by solid lines in FIG. 3 indicate movement directions of air introduced by heat exchange from the heat exchange unit 400
  • arrows indicated by dashed lines indicate movement directions of air introduced from the outside without heat exchange.
  • reference numeral 107 denotes air introduced from the outside without heat exchange
  • reference numeral 700 denotes a support frame for supporting the reactor 100.
  • first and second air supply assemblies 200 and 300 and the heat exchange unit 400 are provided in the reactor 100.
  • the reactor 100 generates biogas 108 and syngas from biomass 108 by injecting biomass 108 and air as an oxidant from the upper side, and the upper side of the inner space in which the biomass 108 is filled.
  • the drying zone 101, the pyrolysis zone 102, the oxidation zone 103, the combustion zone, and the reduction zone 104 are sequentially formed.
  • the first air supply assembly 200 is spaced apart along the outer surface of the reactor 100 so as to penetrate downward from the upper side of the reactor 100 to extend to the oxidation region 103, and for combustion of the biomass 108.
  • a plurality of things supply air to the oxidation region 103.
  • the second air supply assembly 300 is disposed to be spaced apart along the outer surface of the reactor 100 so as to penetrate downward from the upper side of the reactor 100 to extend to the oxidation region 103, and the first air supply assembly 200 It is disposed between the adjacent first air supply assembly 200, the plurality of air supply for the combustion of the biomass 108 to the oxidation region 103 more than the first air supply assembly 200.
  • first and second air supply assemblies 200 and 300 can be clearly seen in FIG. 2.
  • first and second air supply assemblies 200 and 300 may be alternately arranged at equal intervals as shown, as well as various modifications and application designs such as asymmetrically disposed on one side.
  • modifications and application designs such as asymmetrically disposed on one side.
  • the heat exchange unit 400 is provided at the gas outlet 106 formed at the lower side of the reactor 100, and exchanges heat by synthesizing the syngas 105 discharged from the reduction zone 104 and air supplied from the outside. It is to let. Accordingly, the present invention can selectively adjust the air supply amount to the oxidation region 103 according to the nature and type of the biomass 108 introduced by the first and second air supply assemblies 200 and 300, It can be applied to a wide range of biomass.
  • the present invention reuses the high sensible heat of the syngas 105 produced and discharged due to the structural characteristics of the top-down gasification method to heat the air necessary for the gasification process by the heat exchange unit 400 again, thereby minimizing unnecessary waste of energy. It is possible to improve the production efficiency of the syngas 105.
  • the reactor 100 is for producing the syngas 105 from the biomass 108 introduced as described above, the reactor upper body 110 and the outer case 120 are largely interconnected, and the inner case 130 is It can be seen that the structure is built in the outer case 120.
  • a brief description will be given of the drying zone 101, the pyrolysis zone 102, the oxidation zone 103 and the reduction zone 104 which are sequentially formed from the upper side in the reactor 100. see.
  • the moisture content in the biomass 108 introduced into the reactor 100 is controlled by combustion heat transfer.
  • gaseous conversion materials such as char or tar are extracted from the inside of the biomass 108 introduced into the reactor 100 by combustion heat transfer.
  • partial combustion by an ignition burner connected to the reactor 100 occurs.
  • Air is introduced through the first and second air supply units 200 and 300, which will be described later, according to types or properties of the biomass 108 introduced to promote partial combustion of the oxidation region 103.
  • the reduction region 104 mainly composed of char (char), pyrolysis gas is converted into hydrogen and carbon monoxide while passing through this region.
  • the reactor upper body 110 is formed in a shape that gradually widens from the upper side, the drying region 101 and the pyrolysis region 102 is formed therein, forming a residence space 511 to temporarily receive the heat-exchanged air
  • the distribution unit 500 is formed in a band shape to surround the outside of the drying area 101 along the upper outer surface.
  • the outer case 120 is connected from the lower edge of the reactor upper body 110, the gas outlet 106 is formed on one side.
  • the inner case 130 is accommodated in the outer case 120, and communicates with the inside of the reactor upper body 110 to form the oxidation region 103 and the reducing region 104 therein.
  • the first air supply assembly 200 and the second air supply assembly 300 which will be described later, are inclined along the upper inner circumferential surface of the inner case 130, respectively.
  • the syngas 105 is discharged from the reduction zone 104 is raised to the gas outlet 106 Guided through, it is preferable that the discharge space 125 is discharged from the reduction zone 104 through the bottom of the inner case 130 is formed.
  • the discharge space 125 is also connected to the ash discharge unit 600 to be described later.
  • the reactor upper body 110, the outer case 120 and the inner case 130 is preferably made of a refractory material excellent in heat insulation.
  • the reactor upper body 110 in more detail it can be seen that the structure including the first fire-resistant wall layer 111 and the fire wall slope 112.
  • the first fireproof wall layer 111 is formed to have a constant thickness from the lower portion of the drying region 101 along the inner circumferential surface of the reactor upper body 110.
  • the fire wall slope 112 is formed to be inclined downward toward the inner case 130 side at the upper end portion of the first fire wall layer 111, and the fire wall slope 112 is introduced into the biomass 108 smoothly to the lower side. It is designed to descend.
  • the structure includes the shaft diameter portion 132 and the enlarged diameter portion 134.
  • the shaft diameter portion 132 includes a combustion slope 131 that is formed to be gradually narrowed from the upper side, and the enlarged diameter portion 134 extends from an edge of the lower end of the combustion slope 131 to be gradually widened.
  • the oxidation region 103 is formed above the shaft diameter portion 132 and the enlarged diameter portion 134, and the reduction region 104 is formed below the enlarged diameter portion 134.
  • Reference numeral w1 denotes the width or diameter of the lower edge of the fire wall slope 112 at the first width
  • reference numeral w2 denotes the width or diameter of the lower edge of the reactor upper body 110 at the second width.
  • Reference numeral w3 denotes the width or diameter of the lower edge of the combustion slope 131 at the third width
  • reference numeral w4 denotes the lower edge of the enlarged diameter portion 134 at the fourth width, that is, the lower edge of the reduction area 104. Represents the width or diameter to be made.
  • the second width (w2) is preferably formed larger than the first width (w1), which is a structure for the biomass 108 introduced from the reactor upper body 110 to be smoothly introduced without a bridge (bridge) phenomenon Because it is.
  • the fourth width w4 is preferably larger than the third width w3 because the ash of the biomass 108 is smoothly discharged from the reduction region 104.
  • the outer diameter of the shaft diameter portion 132 and the enlarged diameter portion 134 includes a second fireproof wall layer 133.
  • the reactor 100 is connected to the upper end of the reactor upper body 110 and at least one or more mounted to each of the hopper 140 and the upper end and the lower end of the hopper 140, which is injected into the biomass 108 is input while rotating Embodiments of the structure further including a torque sensor 150 for detecting a supply amount of the biomass 108 may be applied.
  • the torque sensor 150 When the torque sensor 150 detects the input of the biomass 108 through the hopper 140, the torque sensor 150 rotates to quantitatively control the input amount of the biomass 108 in real time.
  • the air is an oxidant introduced to promote partial combustion of the biomass 108 in the oxidation region 103 and through one or all of the first air supply assembly 200 and the second air supply assembly 300. It is injected into the oxidation region 103.
  • the injected biomass 108 is a wood-based material, such as rice hulls, corn stalks, sawdust, wood chips, etc.
  • about 20% to 35% of the air supply for the complete combustion of the biomass 108 (0.7) ⁇ 0.8 Nm 3 / kg) may be injected, so the first air supply assembly 200 to be described later may be used.
  • the injected biomass 108 when the injected biomass 108 is carbon intensive such as coal and waste and a high molecular material such as petroleum compound, it may be injected about 30 to 50% more than the air supply amount condition of the biomass 108 which is wood-based. 2 may be used as the air supply assembly 300.
  • first and second air supply assemblies 200 and 300 may be applied to various operating methods such as individually or fully operating in view of the above conditions.
  • the structure includes a first main pipe 210, the first valve 220 and the air supply pipe 230.
  • the first main pipe 210 is disposed on an upper outer surface of the reactor 100, ie, the upper part of the reactor 110, and divides the first main pipe 210 to form a retention space 511 in which air heat-exchanged from the heat exchange unit 400 is temporarily received. It is branched from the unit 500 toward the lower side of the reactor 100.
  • first valve 220 opens and closes the flow path in the first main pipe 210, and the air supply pipe 230 extends inclined with respect to the first main pipe 210 to be heat-exchanged in the oxidation region 103.
  • the flow path for injecting air is formed.
  • the second air supply assembly 300 may be understood to have a structure including a second main pipe 310, a second valve 320, and first and second cylinder parts 330 and 340.
  • the second main pipe 310 is disposed on the upper outer surface of the reactor 100, the reactor from the distribution unit 500 to form a residence space 511 to temporarily receive the air heat exchanged from the heat exchange unit 400 therein ( It is branched toward the lower side of 100).
  • the second valve 320 opens and closes the flow path in the second main pipe 310.
  • the first cylinder portion 330 communicates with the second main pipe 310 to form a communication space 335 through which the heat-exchanged air passes.
  • the second cylinder portion 340 is disposed through both ends of the first cylinder portion 330, and the external air supplied from one end portion joins the heat exchanged air passing through the communication space 335 to form a high speed from the other end portion. To be sprayed.
  • the first and second cylinders 330 and 340 naturally use the suction pressure formed in the reactor 100 in the gasification process of the biomass 108 to naturally introduce air introduced from the outside into the reactor 100.
  • a pressure difference is generated due to the wall adhesion phenomenon of the fluid, i.e., the flow of flow, and the main classification is attached to the lower pressure side. Air can be injected into the air.
  • the structure includes a first cylinder body 331 and the guide 332.
  • the first cylinder body 331 is a cylindrical member that accommodates one side of the second cylinder portion 340, the guide 332 extends from the end edge of the first cylinder body 331, the second cylinder portion 340. It wraps around the outer circumferential surface, and is a truncated cone-shaped member inclined at an angle with respect to the outer circumferential surface of the second cylinder portion 340.
  • the air heat-exchanged through the heat exchange unit 400 to be described later is guided along the inclined surface inside the guide 332 to the outside from the other end of the second cylinder portion 340 through the inner circumferential surface of the second cylinder portion 340. It is sprayed by joining air.
  • the structure includes a second cylinder body 342, a coanda orifice (343) and a venturi nozzle (344).
  • the second cylinder body 342 is accommodated in the first cylinder portion 330, one end is a cylindrical member exposed to the outside.
  • the coanda orifice 343 is inclined with respect to the inclined surface of the guide 332 having a truncated conical shape formed at the end edge of the first cylinder portion 330, a plurality of members penetrated along the outer peripheral surface of the other end of the second cylinder body 342 to be.
  • the venturi nozzle 344 extends gradually larger than the second cylinder body 342 so as to be exposed to the outside of the first cylinder part 330 from the other end of the second cylinder body 342.
  • the coanda orifice 343 is preferably disposed proximate to the end edge of the guide 332 to promote wall attachment of the fluid to enhance the coanda effect.
  • the heat exchange unit 400 as described above for the cross-flow flow of the syngas 105 and the air supplied from the outside to exchange heat, the gas conduit 410, the exchange jacket 420 and the air baffle (430, It can be seen that the structure including the air baffle).
  • the gas conduit 410 is connected to the gas outlet 106 and forms a flow path through which the syngas 105 is discharged.
  • the exchange jacket 420 is provided with an air inlet port 421 through which air is introduced from the outside at one side, and the heat exchange toward the residence space 511 of the distribution unit 500 disposed at the upper outer surface of the reactor 100 at the other side.
  • An air discharge port 422 is provided to supply the heat exchanged air from the unit 400, and surrounds the entire outer circumferential surface of the gas conduit 410 and forms an exchange space 415 therein.
  • the air baffle 430 is formed in a spiral shape along the formation direction of the exchange space 415 between the inner circumferential surface of the exchange jacket 420 and the outer circumferential surface of the gas conduit 410. Accordingly, the air introduced through the air inlet port 421 undergoes a sufficient heat exchange with the syngas 105 discharged at a high temperature while causing a retardation flow along the formation direction of the air baffle 430, and then the first air supply assembly ( 100) and the second air supply assembly 200 are supplied to the side.
  • the heat exchange unit 400 has a gas conduit 410 and the exchange jacket 420 has an exchange space 415 in the form of a double pipe to exchange heat with the synthesis gas 105 in which air introduced from the outside is discharged to a high temperature. It can be said that it is prepared in terms of the use of waste heat recovery through.
  • the present invention is disposed on the upper outer surface of the reactor 100, the first air supply assembly 200 and the second air supply assembly while using the air heat exchanged from the heat exchange unit 400 as a heat source of the drying area 101
  • Embodiments of a structure further including a distribution unit 500 for supplying to 300 may be applied.
  • the distribution unit 500 may reduce the combustion load of the biomass 108 in the oxidation region 103 by increasing the temperature of the drying region 101 and the pyrolysis region 102 in the reactor 100, and greatly. It can be seen that the structure includes a distribution jacket 510 and a connection pipe 520.
  • the distribution jacket 510 is formed in a band shape along the upper outer surface of the reactor 100 to form a residence space 511 for temporarily receiving heat-exchanged air.
  • connection pipe 520 communicates the air discharge port 422 and the retention space 511 of the heat exchange unit 400 with each other.
  • the first air supply assembly 200 and the second air supply assembly 300 communicate with the residence space 511 to supply the heat-exchanged air to the oxidation region 103, respectively.
  • the dispensing unit 500 Since the dispensing unit 500 has a direction in which the biomass 108 is injected and a direction in which air is used as an oxidant is the same direction, a structure for increasing the temperature of the drying region 101 and the pyrolysis region 102 is required.
  • the structure of the distribution unit 500 also serves to accelerate the drying of moisture in the biomass 108 and to mitigate the increase in thermal entropy of the (gasification) process of thermally decomposing the biomass 108.
  • the distribution unit 500 is oxidized when the air heat-exchanged and heated through the heat exchange unit 400 is injected into the oxidation region 103 through the first air supply assembly 200 or the second air supply assembly 300. Local combustion of the biomass 108 in the region 103 can be promoted, and productivity of the syngas 105 can be improved.
  • the distribution unit 500 is to play an important role in the gasification reaction apparatus to produce a synthesis gas 105 of 2 to 2.5 Nm 3 per kg of biomass 108 together with the heat exchange unit 400. .
  • the present invention is disposed on the lower side of the reactor 100, and further comprises a ash discharge unit 600 for discharging the remaining ash from the synthesis gas 105 from the reduction zone 104 to the outside of the reactor 100 It is preferable to include.
  • the re-discharge unit 600 includes a drive motor 610, a thrust bearing 621, a drive shaft 620, a grate assembly, a reclosing tank 640, a discharge screw 650, and a discharge motor ( It can be seen that the structure including a 660 and the discharge induction pipe 670.
  • the drive motor 610 is disposed on the bottom of the reactor 100 to transfer the driving force to the drive shaft 620 connected to the drive motor 610, the drive shaft 620 is rotatably supported by the thrust bearing 621, It receives the driving force from the drive motor 610 to rotate.
  • the great assembly 630 is connected to the upper end of the drive shaft 620, is embedded in the lower portion of the reduction zone 104 and rotated at a constant speed while burning the ash of the biomass 108 burned from the reduction zone 104 by a predetermined amount. It is a truncated cone-shaped member in which the disks which formed the some step
  • the great assembly 630 forms a structure in which ash of the biomass 108 may be discharged in a grill or mesh form on the bottom thereof, and interlocks with the drive shaft 620 that rotates intermittently very slowly. Periodically, the ash of the biomass 108 is discharged from the reduction zone 104 by a predetermined amount.
  • the reclosing tank 640 is provided at the bottom of the reactor 100 to form a space for temporarily receiving the ashes of the biomass 108 that has fallen.
  • Discharge screw 650 is formed in a spiral shape along the outer circumferential surface of the discharge shaft 651 is formed to be inclined upward from the bottom of the re-receiving tank 640 to rotate in one direction.
  • the discharge motor 660 is connected to the end of the discharge shaft 651 to transmit a driving force to the discharge shaft 651.
  • the discharge guide pipe 670 extends from the receptacle tank 640 and includes a discharge screw 650, and has a ash discharge port 671 on which ash is discharged.
  • the ashes of the biomass 108 dropped and accumulated in the reclosing tank 640 are conveyed in one direction by the discharging screw 650 as the discharging shaft 651 also rotates when the discharging motor 660 is operated. It is discharged to the outside through the port 671.
  • the outer side of the thrust bearing 621 and the drive shaft 620 is further provided with a cooling jacket 680 having a coolant inlet port 681 through which the coolant flows from the outside and a coolant discharge port 682 through which the coolant is discharged. Therefore, heat generation and overheating of the drive shaft 620 and the thrust bearing 621 may be reduced.
  • the present invention can selectively operate according to the nature and type of the biomass to be introduced and can increase the amount of syngas produced, as well as the temperature of the air supplied to the oxidant by recovering the sensible heat of the syngas discharged. It can be seen that the basic technical idea is to provide a gasification reaction apparatus using biomass that can increase energy efficiency by increasing the energy efficiency and increasing the energy efficiency.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne un réacteur de gazéification utilisant une biomasse, pouvant être mis en œuvre de manière sélective en fonction des caractéristiques et du type de biomasse injectée, augmentant la production de gaz de synthèse, et améliorant en outre l'efficacité de l'énergie pouvant être appliquée au cours d'une étape de gazéification en récupérant encore la chaleur sensible du gaz de synthèse évacué et augmentant la température de l'air fourni en tant qu'agent oxydant.
PCT/KR2014/001057 2013-08-23 2014-02-07 Réacteur de gazéification utilisant une biomasse Ceased WO2015026023A1 (fr)

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KR1020130100364A KR101452327B1 (ko) 2013-08-23 2013-08-23 바이오매스를 이용한 가스화 반응장치
KR10-2013-0100364 2013-08-23

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KR101632146B1 (ko) * 2015-03-31 2016-06-21 (주)정석이엔씨 바이오매스 가스화 장치
KR101632147B1 (ko) * 2015-04-01 2016-06-22 (주)정석이엔씨 바이오매스 발전설비
KR101845858B1 (ko) 2016-09-27 2018-05-18 청우에이스(주) 바이오매스 가스화 시스템, 이를 이용한 바이오매스 가스화 방법 및 바이오매스 가스화를 이용한 발전 시스템
WO2018117864A1 (fr) * 2016-12-20 2018-06-28 Pfs Technology Limited Gazéifieur comprenant un appareil de rotation et une grille
KR102006445B1 (ko) 2018-04-12 2019-08-01 임승묵 폐기물 및 탄소 자원을 이용하는 상향식 가스화 장치
KR102459294B1 (ko) * 2020-12-15 2022-10-26 (주)리엔텍엔지니어링 유기성 슬러지 가스화 시스템
KR20230109513A (ko) 2022-01-13 2023-07-20 임승묵 연속식 열분해 가스화 장치

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