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WO2010047283A1 - Appareil de carbonisation et procédé de carbonisation - Google Patents

Appareil de carbonisation et procédé de carbonisation Download PDF

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Publication number
WO2010047283A1
WO2010047283A1 PCT/JP2009/067917 JP2009067917W WO2010047283A1 WO 2010047283 A1 WO2010047283 A1 WO 2010047283A1 JP 2009067917 W JP2009067917 W JP 2009067917W WO 2010047283 A1 WO2010047283 A1 WO 2010047283A1
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WO
WIPO (PCT)
Prior art keywords
kiln
carbonization
organic substance
gas
dry distillation
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/JP2009/067917
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English (en)
Japanese (ja)
Inventor
信和 田口
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.)
Liberty Net International
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Liberty Net International
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 Liberty Net International filed Critical Liberty Net International
Priority to CN2009801414815A priority Critical patent/CN102186948A/zh
Priority to JP2010534791A priority patent/JP5480814B2/ja
Publication of WO2010047283A1 publication Critical patent/WO2010047283A1/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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/30—Other processes in rotary ovens or retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • 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
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0273—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using indirect heating
    • 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
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F23G5/165—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber arranged at a different level
    • 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
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases

Definitions

  • the present invention relates to a carbonization apparatus and a carbonization method for carbonizing organic matter including waste materials, livestock excrement, or sludge and the like, and more specifically, indirectly heating the organic matter in the kiln from the outside.
  • the present invention relates to a carbonization apparatus and a carbonization method that perform drying, thermal decomposition, and heat storage in a low oxygen atmosphere or a reducing atmosphere.
  • a carbonization pipe with a screw conveyor inside is installed in the combustion furnace, and the carbonization furnace is configured with the front stage of the carbonization pipe as the drying zone, the middle stage as the carbonization zone, and the latter stage as the activation zone.
  • the carbonized raw material supplied from the raw material supply device is indirectly heated in the carbonization tube, so that drying and water vapor in the previous stage are performed.
  • an apparatus for producing activated carbide that generates activated carbide by generation of carbon, generation of carbonization and pyrolysis gas in the middle stage, activation and activation by steam and pyrolysis gas in the latter stage (see, for example, Patent Document 1). ).
  • the fly ash containing dioxins in the activation / activation process decomposes and detoxifies the dioxins by heat treatment via a dechlorination pipe provided with a screw conveyor inside separately from the carbonization pipe.
  • the atmosphere gas is reduced or a low oxygen atmosphere as a condition for detoxifying (dechlorinating) the ash (dioxin decomposition condition).
  • the activated carbide production apparatus configured as described above, not only the raw material type is limited, but also the carbide obtained through the two-stage production process of carbonization reaction and activation reaction is activated carbon with a small specific surface area. However, it is unsuitable for fuel use and the purpose of use is limited, and the energy of carbide (activated carbon) is also low.
  • an object of the present invention is to provide a reductive carbonization system capable of generating high-energy regenerated coal using a wide range of raw materials.
  • the invention according to claim 1 is a carbonization apparatus that performs drying, pyrolysis, and heat storage of organic matter in one kiln, A rotatable kiln having an inlet and an outlet; A raw material supply unit for introducing an organic substance into the kiln from the inlet; A combustion chamber having the kiln in an internal space and supplying heat to the kiln from the outside; Have The organic matter having a high moisture content is a carbonization apparatus characterized in that the residence time in the kiln is longer than that of the organic matter having a low moisture content.
  • the drying process and the carbonization process can be continuously performed inside one kiln, and the organic matter and the like put inside one kiln can be reduced in an oxygen-free atmosphere.
  • Indirect heating in a state can promote self-combustion associated with indirect thermal decomposition of organic matter and the like, and a wide range of utilization purposes and high-energy regenerated coal can be produced regardless of a wide variety of raw materials.
  • the invention according to claim 2 is the carbonization apparatus according to claim 1, wherein the organic substance containing a predetermined amount or more of water is conveyed while being repeatedly advanced and returned.
  • the invention according to claim 3 is characterized in that the inner peripheral surface of the kiln has spiral blades extending spirally along the longitudinal direction of the kiln and has at least one stirring blade protruding inward.
  • Item 3 The carbonization apparatus according to Item 1 or 2.
  • the invention according to claim 4 is the carbonization apparatus according to claim 3, wherein the distance between the stirring blades in the longitudinal direction is larger on the upstream side than on the downstream side.
  • the invention according to claim 5 is a connected two- or three-unit structure that separates the water vapor generated inside the kiln from the specific gravity by using a distillate gas having a lighter specific gravity or a higher specific gravity.
  • the reductive carbonization apparatus according to claim 1, comprising: a piping portion.
  • water vapor generated inside the kiln using a difference in specific gravity by two or three pipe parts and lighter specific gravity than this water vapor or heavy specific gravity By separating the gas and the like, hydrogen gas lighter than water vapor, carbon monoxide, methane gas, hydrocarbon gas and the like heavier than water vapor can be separated from the water vapor.
  • the water vapor generated inside the kiln is cooled by separating the water vapor generated inside the kiln into an odor gas and water, and the cooling unit is connected to and separated from the cooling unit.
  • odor gas can be deodorized in the deodorizing section.
  • the invention according to claim 7 has a recovery chamber having an inlet communicating with the outlet of the kiln and an outlet communicating with the combustion chamber. It is.
  • the dry distillation gas recovery chamber by recovering the dry distillation gas generated inside the kiln by the thermal decomposition accompanying carbonization in the carbonization part by the dry distillation gas recovery chamber, The recovered fuel energy can be reused as a heat source for the combustion chamber.
  • the invention according to claim 8 is provided with an auxiliary heating source provided in the dry distillation gas recovery chamber so as to be heated when the amount of heat of the dry distillation gas recovered in the dry distillation gas recovery chamber is insufficient.
  • the reduction carbonization processing system according to any one of claims 1 to 5.
  • the amount of heat when the amount of heat of the dry distillation gas recovered in the dry distillation gas recovery chamber is insufficient is compensated by the auxiliary heating source provided in the dry distillation gas recovery chamber. be able to.
  • the invention according to claim 9 is a method of cooling the smoke that has been collected and the vapor smoke path that collects smoke generated in the early stage of carbonization of the organic matter or the like in the vicinity of the end of the drying unit or in the vicinity of the start of the carbonization unit.
  • oil is recovered after collecting smoke generated at an early stage of carbonization of organic matter or the like in the vicinity of the terminal end of the drying unit or in the vicinity of the start end of the carbonizing unit by a vapor smoke path.
  • Recycled oil can be generated by cooling and oiling the smoke collected by the conversion unit.
  • the cooling unit includes a water distribution pipe for draining water vapor generated inside the kiln and a fan for promoting drainage so as to quickly reduce the moisture content of organic matter and the like.
  • the reduction carbonization processing apparatus according to any one of claims 7 to 9, characterized in that.
  • the cooling unit includes an exhaust pipe that exhausts water vapor generated inside the kiln and a fan for promoting exhaust, so that the moisture content of organic matter and the like is increased. Can be reduced at an early stage, and it can contribute to shortening drying and carbonization time and promoting self-combustion.
  • the invention according to claim 11 uses the reduction carbonization processing system according to any one of claims 1 to 10, throws organic matter containing waste into the one kiln, and puts the one kiln into the one kiln.
  • Reduced carbonization characterized by carbonizing by indirect thermal decomposition of organic matter etc. after reducing the water content by storing the organic matter etc. while indirectly heating the input organic matter etc. in the reduced state of oxygen-free atmosphere Is the method.
  • high energy regenerated coal can be generated using a wide range of raw materials.
  • the invention according to claim 12 is a carbonization method for performing drying, pyrolysis and heat storage of organic matter in one rotary kiln, Introducing an organic substance into the kiln, heating the organic substance in the kiln from outside the kiln,
  • the organic matter having a high water content is a carbonization method characterized in that the carbonization treatment is performed while the residence time in the kiln is longer than the organic matter having a low water content.
  • the invention according to claim 13 is the carbonization method according to claim 12, wherein the organic matter containing a predetermined amount or more of water is conveyed while being repeatedly advanced and returned.
  • the invention according to claim 14 is characterized in that the staying time is performed by changing the height of the stirring blade provided on the inner peripheral surface of the kiln and the interval in the longitudinal direction in accordance with the water content and the input amount of the organic matter.
  • the invention according to claim 15 is characterized in that dry distillation gas generated by decomposition of organic matter in the kiln is combusted in a recovery chamber, and organic matter in the kiln is heated from outside the kiln by heat generated by combustion. 12.
  • the invention according to claim 16 is characterized in that the combustion in the recovery chamber is carried out by introducing air into the recovery chamber without using an external burner. Method.
  • the dry distillation gas recovered in the dry distillation gas recovery chamber has the following auto-ignition temperature. Hydrogen (self-ignition temperature: 560 to 600 ° C.), carbon monoxide (self-ignition temperature: 600 ° C. to 650 ° C.), methane (self-ignition temperature: 630 ° C. to 670 ° C.).
  • Hydrogen self-ignition temperature: 560 to 600 ° C.
  • carbon monoxide self-ignition temperature: 600 ° C. to 650 ° C.
  • methane self-ignition temperature: 630 ° C. to 670 ° C.
  • air is supplied in a state where the whole meets or exceeds the self-ignition temperature and the dry distillation gas starts to burn.
  • actual ignition occurs at much lower temperatures. That is, even if the whole does not reach the self-ignition temperature, the dry distillation gas starts to combust when the self-ignition temperature is locally reached.
  • the invention according to claim 17 is the carbonization method according to any one of claims 12 to 16, wherein drying is performed by setting the inside of the kiln to 180 ° C or lower.
  • Pyrolysis starts from a state in which the kiln is at 180 ° C. or higher.
  • drying is performed at a temperature lower than that, drying in a reducing atmosphere is realized.
  • the only gas that is generated is water vapor and odor gas emitted from organic substances containing moisture. Therefore, the volume of generated gas can be minimized. Therefore, since the volume of the target gas to be deodorized is small, it can be deodorized at a low running cost by other drying methods.
  • the amount of generated gas will increase, a volume will increase, and the process of odor gas will become large.
  • the upstream open end of the kiln is covered so as to be shut off from the outside, and the steam / distilled gas from the upstream open end flows through the connection pipe to the gas recovery section.
  • the carbonization apparatus according to any one of claims 1 to 11, wherein an intake blower capable of arbitrarily adjusting an intake air amount is provided in the middle of the connection pipe.
  • the carbonization processing system of the present invention can generate high energy regenerated coal using a wide range of raw materials.
  • Example shown below is a suitable specific example in the reductive carbonization apparatus of this invention, the carbonization method, and a rice husk charcoal oil adsorbent,
  • various technically preferable restrictions such as numerical limitation and material limitation, are shown.
  • the technical scope of the present invention is not limited to these embodiments unless specifically described to limit the present invention.
  • FIG. 1 is an explanatory view of a reduction carbonization processing system according to an embodiment of the present invention
  • FIG. 2 is a cross-sectional view of a kiln in the reduction carbonization processing system according to an embodiment of the present invention.
  • a reduction carbonization apparatus 1 applied to a reduction carbonization system is a method for drying input material (rice husk P) inside one substantially cylindrical kiln 2.
  • -It is configured to perform each process of pyrolysis (carbonization) and heat storage.
  • the reduction carbonization apparatus applied to the reduction carbonization system has an inlet 2in and an outlet 2out, and drying, pyrolysis (carbonization), and heat storage of rice husk P in a series of internal spaces 2c. 1 in this order, a supply unit for storing a large amount of rice husk P as a raw material and supplying the rice husk P sequentially from the inlet 2in to the internal space 2c, and heating the internal space 2c from the outside of the kiln 2.
  • the combustion chamber 3, the exhaust part 5 for exhausting the air contained in the rice husk P supplied from the supply part to the inlet 2in, and the carbonized rice husk charcoal Q discharged from the outlet 2out are recovered and the outside air to the outlet 2out is recovered.
  • the supply unit includes a hopper 14 storing rice husk P as an input material to be carbonized, a supply pipe 15 connected to the hopper 14 and having an elbow shape so that one end faces the internal space 2c from the inlet 2in, And a supply screw 16 arranged along the horizontal axis direction of the pipe 15 to maintain an oxygen-free atmosphere (including a low oxygen atmosphere) in the vicinity of the inlet 2in side of the internal space 2c.
  • a supply screw 16 arranged along the horizontal axis direction of the pipe 15 to maintain an oxygen-free atmosphere (including a low oxygen atmosphere) in the vicinity of the inlet 2in side of the internal space 2c.
  • the combustion part has a casing-like main body that forms a combustion chamber 3 that surrounds the whole except for the inlet 2in and the outlet 2out formed at both ends of the kiln 2, and the vicinity of the upper portion of the outlet 2out so as to communicate with the combustion chamber 3.
  • An exhaust pipe 3a having one end connected to the exhaust pipe 3a, a chimney 23 connected to the other end of the exhaust pipe 3a and communicating with the outside, a combustion chamber in the vicinity of the upper end of the inlet 2in with one end connected to the chimney 23 and the other end 3, a circulation pipe 24 connected to the main body so as to communicate with the main body 3, a heating source 4 such as a burner facing the combustion chamber, and a fan 13 for promoting exhaust.
  • the combustion unit can store heat in the rice husk P while indirectly heating the rice husk P supplied to the internal space 2c in a reduced state in an oxygen-free atmosphere, and supply heat to the entire one internal space 2c.
  • the exhaust unit 5 includes a water vapor exhaust pipe 12 for draining water vapor generated inside the kiln 2 and a fan 13 for promoting exhaust so that the moisture content of the rice husk P is lowered early.
  • the exhaust part 5 can reduce the moisture content of the rice husk P at an early stage by cooperation with the steam exhaust pipe 12 disposed below and the exhaust promoting fan 13 disposed inside the main body. It can contribute to shortening drying and carbonization time and promoting self-combustion.
  • a cooling device such as a cooling pipe is disposed around the recovery unit 60, and the rice husk P can be generated (recovered) as regenerated charcoal by this cooling.
  • the outlet 2out of the kiln 2 and the recovery unit 60 are connected so as to maintain an oxygen-free atmosphere (including a low oxygen atmosphere) in the internal space 2c.
  • the collection unit 60 is disposed below the outlet 2out of the kiln 2, is connected so as to collect the rice husk charcoal Q by falling under its own weight, and is piped in the depth direction of FIG.
  • the kiln 2 is installed horizontally on the left and right side walls of the combustion chamber 3 at both ends.
  • the kiln 2 is a metal tubular rotating body arranged in the combustion chamber 3, and a sprocket around which a chain extending from the drive device is wound is provided on the inlet 2in side, although not shown. It can be rotated by driving the drive device.
  • the inlet 2in side of the kiln 2 is covered with an exhaust part 5 for exhausting the air contained in the rice husk P supplied from the supply part 30 to the inlet 2a and at the same time releasing the steam generated by the carbonization treatment from the steam vent pipe 22. It has been broken.
  • outlet 2out side of the kiln 2 is a discharge section (connection) for discharging rice husk charcoal Q that has been heated and carbonized and discharging primary combustion gas (combustible gas containing CO) from the degassing pipe 25. Tube) 19.
  • the drying process and the carbonization process can be continuously performed inside one kiln 2, and the rice husk P introduced into one kiln 2 is indirectly heated in a reduced state in an oxygen-free atmosphere.
  • the self-combustion associated with the indirect thermal decomposition of the rice husk P can be promoted, and the high-energy rice husk charcoal Q having a wide use purpose can be generated.
  • a reduction carbonization processing apparatus includes a rotating kiln 2 in which a spiral blade and a stirring blade 1 are arranged, and an interior of the one kiln 2.
  • a combustion chamber 3 that stores the organic matter including the waste that has been thrown into the organic material while indirectly heating in a reduced state in an oxygen-free atmosphere and supplies heat to the entire interior of one kiln 2;
  • a heating source 4 such as a burner, a drying unit 2a having an area set inside the kiln 2 so as to evaporate water contained in the organic matter and the like introduced into the kiln 2 by indirect heating of the combustion chamber 3, and drying A carbonized portion 2b having an area set inside the kiln 2 so as to be carbonized by indirectly heating and decomposing the organic matter and the like dried in the portion 2a.
  • the internal space 2c of the kiln 2 is located between the spiral wing 1a and the spiral wing 1a as shown in FIG. And a stirring blade 1b protruding toward the surface.
  • sections 2a, 2b, and 2d for performing drying, pyrolysis (carbonization), and heat storage steps from the upstream side to the downstream side in the transport direction from the inlet 2in to the outlet 2out are set.
  • the pitch interval of the spiral wing 1a is made different in each of the sections 2a, 2b, 2d, and the pitch interval is narrowed toward the downstream side in the transport direction, whereby the residence time of the rice husk P in the internal space 2c is downstream in the transport direction.
  • the pitch interval of the spiral blade 1a is set so that the residence time is increased stepwise in units of the sections 2a, 2b, and 2d in the order of the processes of drying, pyrolysis (carbonization), and heat storage.
  • the drying unit 2a is a drying section that performs drying affirmation to reduce the moisture content to a state where the moisture contained in the rice husk P is evaporated by indirect heating of the combustion chamber 3 and can be carbonized.
  • the carbonization part 2b is a carbonization section that performs a carbonization process in which the chaff P after the drying process is carbonized (thermally decomposed) in an oxygen-free atmosphere by indirect heating of the combustion chamber 3.
  • the heat storage section 2d is a heat storage section in which heat energy is accumulated in the husk charcoal Q after carbonization by indirect heating of the combustion section 4 and a heat storage process is performed to increase the thermal efficiency of drying and carbonization inside the kiln 2.
  • Fig. 2 shows the basic operation of each process performed in the kiln.
  • the first process is a drying process.
  • the water content is reduced to a state where water contained in the input material is evaporated by indirect heating and can be carbonized.
  • the next process is a carbonization process.
  • the dried material is carbonized (thermally decomposed) in an oxygen-free atmosphere by indirect heating.
  • the next process is a heat storage process.
  • This step is a step for accumulating indirectly heated thermal energy in the carbide and increasing the thermal efficiency of drying and carbonization inside the kiln.
  • the carbonization processing system of the present invention is a connected two-line system that separates water vapor generated inside the kiln 2 from a gas having a lower specific gravity or a higher specific gravity using the difference in specific gravity. It is preferable to provide a triple piping section.
  • the gas to be deodorized mainly contains water vapor and odor gas. That is, it contains almost no carbonization gas. Therefore, it is possible to perform the deodorizing process with the minimum volume. As a result, the deodorizing process can be performed at low cost.
  • hydrogen gas lighter than water vapor, carbon monoxide, methane gas, hydrocarbon gas, etc. heavier than water vapor can be separated from water vapor.
  • the cooling part 6 which isolate
  • a deodorizing unit 7 for deodorizing.
  • the steam generated in the kiln 2 is cooled by the cooling unit 6 to separate the steam generated in the kiln 2 into odor gas and water, thereby deodorizing the odor gas. It can be performed in the deodorizing unit 7.
  • a dry distillation gas recovery unit 8 that recovers dry distillation gas generated inside the kiln 2 by pyrolysis accompanying carbonization in the carbonization unit 2 b is provided, and the fuel energy recovered by the dry distillation gas recovery unit 8 is used as a heat source for the combustion chamber 3. Reuse as.
  • the fuel recovered by the dry distillation gas recovery unit 8 is recovered by recovering the dry distillation gas generated in the kiln 2 by the pyrolysis accompanying carbonization in the carbonization unit 2b by the dry distillation gas recovery unit 8.
  • the energy can be reused as a heat source for the combustion chamber 3.
  • an auxiliary heating source 9 is provided inside the dry distillation gas recovery unit 8 so as to heat the dry distillation gas recovered in the dry distillation gas recovery unit 8 when the amount of heat is insufficient.
  • the amount of heat when the amount of heat of the dry distillation gas recovered in the dry distillation gas recovery unit 8 is insufficient can be supplemented by the auxiliary heating source 9 provided in the dry distillation gas recovery unit 8.
  • route 10 which collect
  • the oily unit 11 collects the smoke. Smoke can be cooled and oiled to produce recycled oil.
  • the cooling unit 6 includes an air distribution pipe 12 that exhausts water vapor generated inside the kiln 2 and an exhaust promotion fan 13 so as to quickly reduce the moisture content of organic substances and the like.
  • the cooling unit 6 includes the air distribution pipe 12 that exhausts the water vapor generated inside the kiln 2 and the exhaust promotion fan 13. It can be reduced early, and can contribute to shortening drying and carbonization time and promoting self-combustion.
  • the following structure may be used for an organic substance having a high moisture content in order to make the residence time in the kiln 2 longer than that of an organic substance having a low moisture content.
  • Fig. 5 shows an example of this.
  • the inner peripheral surface of the kiln 2 has spiral blades 1a extending spirally along the longitudinal direction of the kiln 2 and one or more stirring blades 1b protruding inward.
  • the spiral wing 1a is formed by attaching a strip-shaped thin plate to the inner peripheral surface of the kiln 2 in a spiral. It is preferable that the protrusion amount h of the spiral feather 1a from the inner peripheral surface of the kiln 2 is larger than the protrusion amount at the drying portion B than the protrusion amount at the decomposition portion C. In the drying part B, 0.5 to 0.7 is preferable. The same applies to the protruding amount of the stirring blade 1b. In addition, you may enlarge gradually toward the decomposition
  • a plurality of stirring blades 1b may be provided.
  • an inclination of 60 ° is provided in the counterclockwise direction with reference to the line connecting the center.
  • the distance between the pitches of the spiral wings 1a is made larger on the upstream side than on the downstream side. Thereby, the supply amount of the organic substance into the kiln can be maximized.
  • the stirring blade 1b may be provided continuously in the longitudinal direction of the kiln 2 or may be provided intermittently. What is necessary is just to select suitably in consideration of the ease of manufacture.
  • An organic substance having a high water content is an organic substance having a high adhesiveness
  • an organic substance having a low water content is an organic substance having a low adhesiveness
  • FIG. 6A shows the case where the water content is high
  • FIG. 6B shows the case where the water content is low.
  • the organic matter falls after being lifted to a high position.
  • the organic substance falls at a low position.
  • the time spent in the drying process becomes longer.
  • the time spent in the drying process is shortened.
  • the difference in the staying time can be further increased if the distance between the stirring blades in the longitudinal direction is larger on the upstream side than on the downstream side.
  • FIG. 14 shows an apparatus according to another embodiment.
  • the upstream opening end of the kiln 2 is covered so as to be blocked from the outside, and the water vapor / dry distillation gas from the upstream opening end is caused to flow through the connection pipe 27 to the gas recovery unit 29 of the heat recovery facility.
  • a line is provided, and an intake blower capable of arbitrarily adjusting the intake air amount is provided in the middle of the connection pipe 27.
  • the downstream opening end of the kiln 2 is covered so as to be blocked from the outside, and gas (mainly dry distillation gas) from the downstream opening end is supplied to the gas recovery section 29 of the heat recovery section via the connection pipe 27.
  • gas mainly dry distillation gas
  • the line between the connection pipe 27 and the gas recovery unit 29 is a parallel line, and a damper capable of adjusting the exhaust amount is provided in the middle of each parallel line.
  • Intake tatami In addition to the dry distillation gas generated by thermal decomposition, if there is a large amount of water vapor, it becomes difficult to smoothly discharge the gas. In order to efficiently discharge this water vapor from the kiln 2 and lead it to a heat recovery combustion facility, Intake tatami can be adjusted arbitrarily, an intake air heater is installed, an exhaust pipe that leads dry distillation gas to the heat recovery combustion facility, and an exhaust pipe that mainly leads water vapor to the heat recovery combustion facility are installed in parallel to adjust the displacement of each. It is effective to install a damper that can be used.
  • the amount of intake air can be arbitrarily adjusted with respect to the carbonized material having a high water content, and steam can be efficiently and quickly discharged from the kiln to increase the carbonization efficiency in the kiln.
  • a water jacket is provided outside the second discharge pipe 19 in the recovery unit 60, and a water jacket is also provided around the heat recovery combustion facility to prevent overheating.
  • the organic matter P including waste is supplied from the hopper 14 and supplied to the raw material supply pipe 15 connected so as to maintain the oxygen-free atmosphere (including the low oxygen atmosphere) of the kiln 2 on the start end side of the kiln 2. It is fed into the kiln 2 by a screw 16.
  • the rotatable kiln 2 is carbonized from the drying unit 2a through the carbonization unit 2b by the action of the blades provided on the inner surface of the kiln 2 while rotating through a known drive system. Recycled charcoal Q carbonized in the section is discharged (collected) via the discharge pipe 17.
  • a cooling device 18 such as a drain pipe is disposed around the discharge pipe 17, and by this cooling, organic carbide or inorganic carbide is generated (recovered) as regenerated coal according to the type of organic matter P or the like. .
  • the end portion of the kiln 2 and the discharge pipe 17 are connected so as to maintain an oxygen-free atmosphere (including a low oxygen atmosphere) of the kiln 2.
  • the discharge pipe 17 is disposed below the end portion of the kiln 2 and is connected so as to collect carbides by falling due to its own weight, and is connected in the depth direction of FIG. 19 and the conveying screw 20 provided in the connecting pipe 19 dispose the carbides conveyed by the conveying screw 20 from the inside and outside (atmosphere) of the kiln 2.
  • the conveying screw 21 also inside the discharge pipe 17.
  • a reducing pipe 19 is provided at the start end side and the terminal end side of the kiln 2, and a dry distillation gas recovery part 8 that also serves as the deodorizing part 7 is connected to the reduction pipe 19, and this dry distillation gas recovery part Part of the dry distillation gas recovered in 8 is reused as a heat source for the combustion chamber 3, and the other part is exhausted from the exhaust pipe 3a.
  • the dry distillation gas recovered from the inside of the kiln 2 is basically in a high temperature environment.
  • the temperature of the dry distillation gas is increased by the heating of the auxiliary heating source 9 so as to maintain a temperature suitable for the kind of P (equivalent to the self-ignition temperature).
  • a water distribution pipe 12 that also serves as a vapor smoke path 10 (or may be provided separately) is provided below the start end side of the kiln 2 via two pipe sections 5, and is generated inside the kiln 2. Of the water vapor, aerating water as water is collected.
  • Aeration water is a liquid obtained by cooling the smoke generated in the initial stage of carbonization.
  • organic matter P is mainly wood chips
  • the regenerated charcoal is 25% of the weight of the wood. 20-30% aeration water can be collected with respect to the weight.
  • the collected air mist is cooled (for example, for one month or more), it is separated into a wood tar, a wood vinegar solution, and a light oil, and a recycled fuel or the like can be collected.
  • wood vinegar liquid (vinegar liquid) contains over 200 kinds of components such as alcohols and phenols, and products such as deodorants, human waste treatment agents, pharmaceuticals, animal feed additives, agriculture and forestry, etc. And can be reused in various fields.
  • Wood tar is a pyrolysis liquid of hydrocarbon (lignin), and is a precipitate that is generated when air spilled water is cooled and left for about one month or more. It has strong sterilizing power and can be used as a deodorant. In addition, it can be divided into light oil, heavy oil, and pitch as fuel or as it is further separated into water and oil with a distillation device.
  • hydrocarbon lignin
  • dioxins and odors are removed from the odor gas introduced from the piping unit 5 to the deodorization unit (deodorization / detoxification combustion device) 7 under an environment of 850 to 1000 ° C.
  • a tertiary combustion chamber 22 is disposed in connection with the deodorizing unit 7, and this tertiary combustion chamber 22 cleans the emulsion at 70 to 120 ° C. (low temperature harmless) ) May also be achieved.
  • Emulsion purification is a mixture of microscopic water droplets that are uniformly distributed in high-temperature flammable gas or oil.
  • the gas (oil droplets) that removes the water droplets is also refined to improve the mixing with the air, whereby the gas and oil can be completely burned.
  • the gas and oil components become superfine during the emulsion combustion, the contact area with the air can be increased, and complete combustion can be achieved, greatly reducing the generation of unburned material and reducing dust. Can be significantly reduced.
  • the particles become fine particles due to the micro-explosive action, so that low O2 combustion operation can be realized, and more complete combustion can be achieved, so that only the amount of dust in the exhaust gas can be achieved. no, it is possible to significantly reduce the NO x and sO x and the like.
  • waste materials / plastics for example, as shown in FIG. 3, waste materials / plastics, medical waste (3 cm or more), wood chips / sawdust (less than 3 cm), livestock feces (moisture content less than 60%) It can be applied to a wide range of waste materials such as food residue, livestock dung (water content 60% or more), sludge (after concentration / dehydration), etc. It is supplied to the kiln 2 after performing ultra-dehydration treatment.
  • a high temperature environment of 850 ° C. could be realized, and combustion could be completed in a residence time of 2 seconds or more.
  • the spiral blade and the stirring blade 1 are separated so that they can be independently driven by the drying unit 2a and the carbonizing unit 2b, or the carbonized unit 2b has a narrower pitch than the drying side 2a. It is also possible to clearly divide roles within one kiln 2. At this time, appropriate design changes, exchanges, and the like can be arbitrarily performed such as double spiraling of the spiral wings and changing the spiral shape (angle and maximum diameter).
  • the processing capacity can be returned, depending on the raw material used (such as organic matter P). Therefore, it is possible to employ a product having an appropriate capacity.
  • the inner diameter of the kiln 2 is 500 ⁇
  • the organic matter P has a size of about 3 cm or less, a moisture content of 10% to 60%, a bulk specific gravity of about 0.5, a residence time until carbonization of 30 minutes or less, It is preferable that
  • a dry distillation gas outline calculation sheet (not shown) or the like, a combustion characteristic table of the dry distillation gas (self ignition temperature list), or the like in advance.
  • the calorific value of coal is 7,190 Kcal / kg
  • the calorific value of wood is 3,440 Kcal / kg.
  • the organic matter P containing waste is put into one kiln 2 and the organic matter put into one kiln 2 is put into an oxygen-free atmosphere. It is possible to produce high energy regenerated coal using a wide range of raw materials by carbonizing by indirect heating and decomposition of organic matter etc. after storing heat in organic matter etc. while indirectly heating in reduced state and reducing moisture content. it can.
  • FIGS. 1-10 The micrographs of the above regenerated coal are shown in FIGS.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Treatment Of Sludge (AREA)
  • Processing Of Solid Wastes (AREA)
  • Muffle Furnaces And Rotary Kilns (AREA)
  • Coke Industry (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

L'invention concerne un système de réduction et de carbonisation, dans lequel un large éventail de matières premières peut être utilisé pour produire du carbone régénéré ayant une énergie élevée. Le système est un appareil de carbonisation dans lequel une substance organique est séchée et pyrolysée dans un four (2) et la chaleur est stockée dans le même four. L'appareil est caractérisé en ce qu'il comprend un four rotatif (2) ayant une entrée et une sortie, un dispositif d'alimentation en matière première destiné à introduire une substance organique dans le four (2) par l'entrée, et une chambre de combustion (3) qui contient le four (2) dans son espace interne et fournit de la chaleur au four (2) depuis l'extérieur, et en ce qu'il est configuré de manière à ce qu'une substance organique ayant une teneur en eau élevée réside dans le four (2) pendant une durée plus longue qu'une substance organique ayant une faible teneur en eau. L'appareil est également caractérisé en ce que le four (2) comprend, sur la surface circonférentielle interne, une lame en spirale (1a) qui s'étend en spirale dans la direction longitudinale du four (2) et une ou plusieurs lames d'agitation (1b) qui s'étendent vers l'intérieur.
PCT/JP2009/067917 2008-10-20 2009-10-16 Appareil de carbonisation et procédé de carbonisation Ceased WO2010047283A1 (fr)

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JP2016093811A (ja) * 2010-02-02 2016-05-26 株式会社ガイア環境技術研究所 油乃至ガス吸着材の製造方法及び油乃至ガス吸着材
CN104258438B (zh) * 2014-10-16 2017-01-04 史金麟 一种生活垃圾除臭的方法及其装置
JP2017517384A (ja) * 2014-04-15 2017-06-29 フラウンホーファー−ゲゼルシャフト ツル フェルデルング デル アンゲヴァンテン フォルシュング エー ファウＦｒａｕｎｈｏｆｅｒ−Ｇｅｓｅｌｌｓｃｈａｆｔ ｚｕｒ Ｆｏｅｒｄｅｒｕｎｇ ｄｅｒ ａｎｇｅｗａｎｄｔｅｎ Ｆｏｒｓｃｈｕｎｇ ｅ．Ｖ． 材料を熱接触処理する装置及び方法及びそれにより製造された熱分解油
JP2018053197A (ja) * 2016-09-30 2018-04-05 東日本高速道路株式会社 熱分解システム及び熱分解方法
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JP6002877B2 (ja) * 2010-02-02 2016-10-05 株式会社ガイア環境技術研究所 油乃至ガス吸着材の製造方法及び油乃至ガス吸着材
JP2014500892A (ja) * 2010-10-26 2014-01-16 西峡龍成特種材料有限公司 加熱ガス循環式炭材分解方法および設備
JP2012206011A (ja) * 2011-03-29 2012-10-25 Gaia Kankyo Gijutsu Kenkyusho:Kk 浄水材及びその使用方法、ならびにその製造方法
JP2013117524A (ja) * 2011-10-31 2013-06-13 Gaia Institute Of Environmental Technology Inc 放射性物質を吸収及びろ過する炭化物の製造方法及びその利用方法、並びに浄水器、及び水処理装置、及び機能性食品
JP2014121698A (ja) * 2012-11-22 2014-07-03 Gaia Institute Of Environmental Technology Inc 多孔質炭の凝集助剤、及び多孔質炭のろ過助剤、及び水処理方法
CN103834418B (zh) * 2014-04-02 2015-06-10 青岛伊诺威能源化工新技术有限公司 横向交替加热、竖向排焦式捣固炼焦炉
CN103834418A (zh) * 2014-04-02 2014-06-04 青岛伊诺威能源化工新技术有限公司 横向交替加热、竖向排焦式捣固炼焦炉
JP2017517384A (ja) * 2014-04-15 2017-06-29 フラウンホーファー−ゲゼルシャフト ツル フェルデルング デル アンゲヴァンテン フォルシュング エー ファウＦｒａｕｎｈｏｆｅｒ−Ｇｅｓｅｌｌｓｃｈａｆｔ ｚｕｒ Ｆｏｅｒｄｅｒｕｎｇ ｄｅｒ ａｎｇｅｗａｎｄｔｅｎ Ｆｏｒｓｃｈｕｎｇ ｅ．Ｖ． 材料を熱接触処理する装置及び方法及びそれにより製造された熱分解油
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JP2022045221A (ja) * 2020-09-08 2022-03-18 日立造船株式会社 ガス化装置

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MY156263A (en) 2016-01-29
MY169929A (en) 2019-06-17
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