WO2010047283A1 - Apparatus for carbonization and method of carbonization - Google Patents
Apparatus for carbonization and method of carbonization Download PDFInfo
- 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
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- kiln
- carbonization
- organic substance
- gas
- dry distillation
- Prior art date
Links
Images
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.
Landscapes
- 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)
- Gasification And Melting Of Waste (AREA)
- Coke Industry (AREA)
Abstract
Description
入口及び出口を有する回転可能キルンと、
該入口から該キルン内に有機物を導入するための原料供給部と、
該キルンを内部空間に有し、該キルンに外部から熱を供給する燃焼室と、
を有し、
含水率が高い有機物は、含水率の低い有機物よりもキルン内における滞在時間が長くなるようにしたことを特徴とする炭化処理装置である。 The invention according to
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.
該キルン内に有機物を導入し、該キルン内の有機物をキルン外部から加熱し、
含水率が高い有機物は、含水率の低い有機物よりもキルン内における滞在時間が長くしながら炭化処理を行うことを特徴とする炭化処理方法である。 The invention according to
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.
請求項18に係る発明は、前記キルンの上流側の開口端を外部から遮断するように覆うとともに、該上流側の開口端からの水蒸気・乾留ガスを接続パイプを介してガス回収部に流すラインを設け、該接続パイプの途中に吸気量を任意に調整することが可能な吸気ブロワを設けたことを特徴とする請求項1乃至11のいずれか1項記載の炭化処理装置である。
請求項19に係る発明は、前記キルンの下流側の開口端を外部から遮断するように覆うとともに、該下流側の開口端からのガスを前記接続パイプを介してガス回収部に流すラインを設け、
該接続パイプと該回収部との間のラインは並列のラインとするとともに、並列なそれぞれのラインの途中に排気量を調整できるダンパを設けたことを特徴とする請求項18記載の炭化処理装置である。 Pyrolysis (carbonization) starts from a state in which the kiln is at 180 ° C. or higher. When drying is performed at a temperature lower than that, drying in a reducing atmosphere is realized. In the case of such drying, 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. In addition, even if it is 180 degrees C or less, if there exists air in a kiln, the amount of generated gas will increase, a volume will increase, and the process of odor gas will become large.
According to an eighteenth aspect of the present invention, 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
According to a nineteenth aspect of the present invention, there is provided a line for covering the downstream opening end of the kiln so as to be shut off from the outside, and for allowing the gas from the downstream opening end to flow to the gas recovery section via the connection pipe. ,
19. The carbonization apparatus according to
1b 攪拌羽
2…キルン
2a 乾燥部
2b 炭化部
2d 蓄熱部
2c 内部空間
2in 入口
2out 出口
3…燃焼室
3a…排気管
4…加熱源
5…配管部
6…冷却部
7…脱臭部
8…乾留ガス回収部
9…補助加熱源
10…蒸気煙経路
11…油化部
12…配水管
13…ファン
14…ホッパ
15…原料供給配管
16…供給スクリュー
17…第2排出配管
18…冷却装置
19…接続管
20…搬送スクリュー
21…搬送スクリュー
22…蒸気抜きパイプ
23 煙突部
24 循環管
25 ガス抜きパイプ
30 接続部
60 回収部 DESCRIPTION OF
なお、以下に示す実施例は本発明の還元炭化処理装置、炭化処理方法、籾殻炭油吸着材における好適な具体例であり、例えば、数値限定や材料限定等の技術的に好ましい種々の限定を付している場合もあるが、本発明の技術範囲は、特に本発明を限定する記載がない限り、これらの態様に限定されるものではない。 Next, a reduction carbonization processing system according to an embodiment of the present invention will be described with reference to the drawings.
In addition, the 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, For example, 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.
図1は本発明の一実施形態に係る還元炭化処理システムの説明図、図2は本発明の一実施形態に係る還元炭化処理システムにおけるキルンの断面図である。 (Example 1)
FIG. 1 is an explanatory view of a reduction carbonization processing system according to an embodiment of the present invention, and FIG. 2 is a cross-sectional view of a kiln in the reduction carbonization processing system according to an embodiment of the present invention.
乾燥部2aは、籾殻Pに含まれる水分を燃焼室3の間接加熱で蒸発させ、炭化できる状態にまで含水率を下げる乾燥肯定を行う乾燥区間である。 5 and 6, the
The drying
(形態例2)
図14に他の形態例に係る装置を示す。
本例では、キルン2の上流側の開口端を外部から遮断するように覆うとともに、上流側の開口端からの水蒸気・乾留ガスを接続パイプ27を介して熱回収設備のガス回収部29に流すラインを設け、接続パイプ27の途中に吸気量を任意に調整することが可能な吸気ブロワを設けてある。
さらに、キルン2の下流側の開口端を外部から遮断するように覆うとともに、下流側の開口端からのガス(主に乾留ガス)を接続パイプ27を介して熱回収部のガス回収部29に流すラインを設け、
接続パイプ27とガス回収部29との間のラインは並列のラインとするとともに、並列のそれぞれのライン途中に排気量を調整できるダンパを設けてある。
含水率の高い素材を1本のキルン2内で乾燥・炭化を行なう場合、問題となるのは、多量の水蒸気の体積である。大気圧下では、1リットルの水は100。Cで、水蒸気の体積が約1,700リットルになる。また、373。Cでは、水蒸気の体積は約3,400リットルにもなる。
熱分解によって生じる乾留ガスに加えて、多量の水蒸気があると、スムーズなガスの排出が困難になる。この水蒸気を効率的にキルン2内から排出させ、熱回収燃焼設備に導くため、
吸気畳を任意に調整できる、吸気プロワの設置、乾留ガスを熱回収燃焼設備に導く排気管と、主に水蒸気を熱回収燃焼設備に導く排気管を並列に設置し、それぞれの排気量を調整できるダンパーを設置することが効果的である。
これによって、含水率の高い炭化素材に対し、吸気量を任意に調整し、効率的・速やかに水蒸気をキルン内から排出し、キルン内の炭化効率を高めることができる。
本例では、さらに、回収部60において第2排出管19の外部にウオータージャケットを設けてあり、また、熱回収燃焼設備の周囲にもウオータージャケットを設けて過熱の防止を図っている。 Further, in this structure, it is possible to realize optimum regenerated charcoal by changing not only the water content of the organic matter but also the amount of protrusion of the blades depending on the amount of the organic matter supplied into the kiln.
(Example 2)
FIG. 14 shows an apparatus according to another embodiment.
In this example, the upstream opening end of the
Further, the downstream opening end of the
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.
When a material having a high water content is dried and carbonized in one
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
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.
As a result, 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.
In this example, a water jacket is provided outside the
以下、本発明の還元炭化処理システムのより具体的な構成を説明する。廃棄物を含む有機物等Pは、ホッパ14から投入されて、キルン2の始端部側にキルン2の無酸素雰囲気(低酸素雰囲気を含む)を維持するように接続された原料供給配管15の供給スクリュー16によってキルン2内へと供給される。 (Example)
Hereinafter, a more specific configuration of the reduction carbonization processing system of the present invention will be described. The organic matter P including waste is supplied from the
原材料:ジャガイモの殻汚泥(含水率80%)を炭化(60分)したところ、燃料発熱量は1kg当たり5440Kcal/kg(固定炭素率78.5%)
原材料:もみ殻(含水率2%)を炭化(15分)したところ、燃料発熱量は1kg当たり4544Kcal/kg(固定炭素率46.6%、シリカ41.6%)
いずれも高エネルギーを有する再生炭を生成することができた。なお、試験はJIS-Z 7302-2に従って行った。 Ingredients: When carbonized coffee beans (water content 65%) is carbonized (50 minutes), the calorific value of the fuel is 7250 Kcal / kg per kg (fixed carbon rate 81.0%)
Raw material: Carbonization (60 minutes) of potato shell sludge (
Raw material: When rice husk (
All were able to produce regenerated coal with high energy. The test was conducted according to JIS-Z 7302-2.
Claims (19)
- 一つのキルン内で、有機物の乾燥と熱分解と蓄熱を行うようにした炭化処理装置であって、
入口及び出口を有する回転可能キルンと、
該入口から該キルン内に有機物を導入するための原料供給部と、
該キルンを内部空間に有し、該キルンに外部から熱を供給する燃焼室と、
を有し、
含水率が高い有機物は、含水率の低い有機物よりもキルン内における滞在時間が長くなるようにしたことを特徴とする炭化処理装置。 It is a carbonization processing device 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
A carbonization apparatus characterized in that an organic substance having a high water content has a longer residence time in the kiln than an organic substance having a low water content. - 所定量以上の水分を含有する有機物は、進行と戻りを繰り返しながら搬送が行われるようにした請求項1記載の炭化処理装置。 The carbonization processing 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.
- キルンの内周面には、キルンの長手方向に沿って螺旋状に延びる螺旋羽を有するとともに、内方に突出する攪拌羽を一以上有することを特徴とする請求項1又は2に記載の炭化処理装置。 The carbonization according to claim 1 or 2, wherein the inner peripheral surface of the kiln has spiral blades extending in a spiral shape along the longitudinal direction of the kiln and at least one stirring blade protruding inward. Processing equipment.
- 前記攪拌羽の長手方向の間隔は、上流側が下流側よりも大きいことを特徴とする請求項3記載の炭化処理装置。 The carbonization apparatus according to claim 3, wherein an interval in the longitudinal direction of the stirring blades is larger on the upstream side than on the downstream side.
- 比重の違いを利用して前記キルン内部で発生した水蒸気とこの水蒸気よりも比重の軽い、または比重の重い乾留ガス等とを分離する連結された2連または3連の配管部を備えていることを特徴とする請求項1に記載の還元炭化処理装置。 It has two or three connected piping sections that separate the water vapor generated inside the kiln using the difference in specific gravity from dry distillation gas having a lighter specific gravity or a higher specific gravity. The reduction carbonization processing apparatus of Claim 1 characterized by these.
- 前記キルン内部で発生した水蒸気を冷却することによって前記キルン内部で発生した水蒸気を臭気ガスと水とに分離する冷却部と、該冷却部に連接されて分離された臭気ガスを脱臭する脱臭部と、を備えていることを特徴とする請求項1に記載の還元炭化処理装置。 A cooling unit that separates water vapor generated inside the kiln into odor gas and water by cooling the water vapor generated inside the kiln; and a deodorization unit that deodorizes the odor gas separated by being connected to the cooling unit. The reduction carbonization processing apparatus according to claim 1, comprising:
- キルンの出口に連通する入口と、燃焼室に連通する出口とを有する乾留ガス回収室を有することを特徴とする請求項1乃至6のいずれか1項記載の炭化処理装置。 7. The carbonization apparatus according to claim 1, further comprising a dry distillation gas recovery chamber having an inlet communicating with the kiln outlet and an outlet communicating with the combustion chamber.
- 前記乾留ガス回収室に回収した乾留ガスの熱量が不足している際に加熱するように前記乾留ガス回収室に設けられた補助加熱源を備えていることを特徴とする請求項1乃至請求項5に記載の還元炭化処理装置。 The auxiliary heating source provided in the dry distillation gas recovery chamber is provided so as to heat when the amount of heat of the dry distillation gas recovered in the dry distillation gas recovery chamber is insufficient. The reduction carbonization processing apparatus of 5.
- 前記乾燥部の終端部付近又は前記炭化部の始端部付近での有機物等の炭化初期に発生した煙を回収する蒸気煙経路と、回収した煙を冷却することで油化する油化部と、を備えていることを特徴とする請求項1乃至請求項8に記載の還元炭化処理装置。 A vapor smoke path for collecting smoke generated in the early stage of carbonization of an organic substance or the like in the vicinity of the terminal end of the drying unit or in the vicinity of the start end of the carbonization unit, and an oilification unit that is oiled by cooling the collected smoke; The reduction carbonization processing apparatus according to claim 1, wherein the reduction carbonization apparatus is provided.
- 前記冷却部は、有機物等の含水率を早期に低下させるように、前記キルン内部で発生した水蒸気を排気する配気管と、排気促進用のファンとを備えていることを特徴とする請求項7乃至請求項9に記載の還元炭化処理装置。 The said cooling part is provided with the distribution pipe which exhausts the water vapor | steam generate | occur | produced inside the said kiln, and the fan for exhaust_gas | exhaustion so that the moisture content of organic substances etc. may be reduced early. The reduction carbonization processing apparatus of Claim thru | or 9.
- 請求項1乃至10のいずれか1項に記載の還元炭化処理装置を用い、前記一つのキルン内部に廃棄物を含む有機物等を投入し、前記一つのキルン内部に投入された有機物等を無酸素雰囲気の還元状態で間接加熱しつつ有機物等に蓄熱して含水率を低減したうえで、有機物等を間接加熱分解させることで炭化することを特徴とする還元炭化処理方法。 11. The reduction carbonization apparatus according to claim 1, wherein an organic substance containing waste is introduced into the one kiln, and the organic substance or the like introduced into the one kiln is oxygen-free. A reductive carbonization method comprising carbonizing an organic substance or the like by indirectly heating and decomposing the organic substance or the like after storing the organic substance or the like while indirectly heating in a reduced state of the atmosphere to reduce water content.
- 一つの回転キルン内で、有機物の乾燥と熱分解と蓄熱を行うようにする炭化処理方法であって、
該キルン内に有機物を導入し、該キルン内の有機物をキルン外部から加熱し、
含水率が高い有機物は、含水率の低い有機物よりもキルン内における滞在時間が長くしながら炭化処理を行うことを特徴とする炭化処理方法。 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,
An organic material having a high water content is carbonized while a residence time in the kiln is longer than that of an organic material having a low water content. - 所定量以上の水分を含有する有機物は、進行と戻りを繰り返しながら搬送が行われるようにした請求項12記載の炭化処理方法。 The carbonization method according to claim 12, wherein the organic substance containing a predetermined amount or more of moisture is conveyed while being repeatedly advanced and returned.
- 前記滞在時間は、キルンの内周面に設けた攪拌羽の高さ、長手方向の間隔を、有機物の含水量、投入量に応じて変化させて行うことを特徴とする請求項12又は13記載の炭化処理方法。 The said staying time is performed by changing the height of the stirring blade provided in the inner peripheral surface of the kiln and the interval in the longitudinal direction according to the water content of the organic matter and the input amount. Carbonization method.
- 前記キルン内の有機物の分解により発生する乾留ガスを回収室において燃焼させ、燃焼により発生した熱によりキルン内の有機物をキルン外部から加熱することを特徴とする請求項12記載の炭化処理方法。 The carbonization method according to claim 12, wherein a dry distillation gas generated by decomposition of the organic matter in the kiln is combusted in a recovery chamber, and the organic matter in the kiln is heated from outside the kiln by heat generated by the combustion.
- 前記回収室における燃焼は、外部バーナーを用いることなく、回収室に空気を導入して行うことを特徴とする請求項12乃至15のいずれか1項記載の炭化処理方法。 The carbonization method according to any one of claims 12 to 15, wherein the combustion in the recovery chamber is performed by introducing air into the recovery chamber without using an external burner.
- キルン内部を180℃以下に設定することにより乾燥を行う請求項12乃至16のいずれか1項記載の炭化処理方法。 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.
- 前記キルンの上流側の開口端を外部から遮断するように覆うとともに、該上流側の開口端からの水蒸気・乾留ガスを接続パイプを介してガス回収部に流すラインを設け、該接続パイプの途中に吸気量を任意に調整することが可能な吸気ブロワを設けたことを特徴とする請求項1乃至11のいずれか1項記載の炭化処理装置。 The upstream opening end of the kiln is covered so as to be blocked from the outside, and a line for flowing water vapor / dry distillation gas from the upstream opening end to the gas recovery unit through the connection pipe is provided. The carbonization processing apparatus according to claim 1, further comprising an intake blower capable of arbitrarily adjusting an intake air amount.
- 前記キルンの下流側の開口端を外部から遮断するように覆うとともに、該下流側の開口端からのガスを前記接続パイプを介してガス回収部に流すラインを設け、
該接続パイプと該回収部との間のラインは並列のラインとするとともに、並列なそれぞれのラインの途中に排気量を調整できるダンパを設けたことを特徴とする請求項18記載の炭化処理装置。 Covering the downstream opening end of the kiln so as to be blocked from the outside, and providing a line for flowing gas from the downstream opening end to the gas recovery section through the connection pipe,
19. The carbonization apparatus according to claim 18, wherein a line between the connection pipe and the recovery unit is a parallel line, and a damper capable of adjusting an exhaust amount is provided in the middle of each parallel line. .
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2010534791A JP5480814B2 (en) | 2008-10-20 | 2009-10-16 | Carbonization apparatus and carbonization method |
CN2009801414815A CN102186948A (en) | 2008-10-20 | 2009-10-16 | Apparatus for carbonization and method of carbonization |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2008-270247 | 2008-10-20 | ||
JP2008270247 | 2008-10-20 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2010047283A1 true WO2010047283A1 (en) | 2010-04-29 |
Family
ID=42119323
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2009/067917 WO2010047283A1 (en) | 2008-10-20 | 2009-10-16 | Apparatus for carbonization and method of carbonization |
Country Status (4)
Country | Link |
---|---|
JP (2) | JP5480814B2 (en) |
CN (1) | CN102186948A (en) |
MY (2) | MY156263A (en) |
WO (1) | WO2010047283A1 (en) |
Cited By (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2012206011A (en) * | 2011-03-29 | 2012-10-25 | Gaia Kankyo Gijutsu Kenkyusho:Kk | Water purifying material and method for production thereof |
JP2013117524A (en) * | 2011-10-31 | 2013-06-13 | Gaia Institute Of Environmental Technology Inc | Method for manufacturing carbide which absorb and filter radioactive substance and method for using the same, and water purifier, water treatment apparatus and functional food |
JP2014500892A (en) * | 2010-10-26 | 2014-01-16 | 西峡龍成特種材料有限公司 | Heated gas circulation type carbon material decomposition method and equipment |
CN103834418A (en) * | 2014-04-02 | 2014-06-04 | 青岛伊诺威能源化工新技术有限公司 | Transverse alternate heating and vertical coke discharging type tamping coke furnace |
JP2014121698A (en) * | 2012-11-22 | 2014-07-03 | Gaia Institute Of Environmental Technology Inc | Flocculation aid of porous charcoal, filtration aid of porous charcoal and water treatment method |
CN104258438A (en) * | 2014-10-16 | 2015-01-07 | 史金麟 | Method and device for deodorizing domestic waste |
GB2529053A (en) * | 2014-07-03 | 2016-02-10 | Dps Bristol Holdings Ltd | Waste processing apparatus |
JP2016093811A (en) * | 2010-02-02 | 2016-05-26 | 株式会社ガイア環境技術研究所 | Method for producing oil and gas adsorbent, and oil and gas adsorbent |
CN104258438B (en) * | 2014-10-16 | 2017-01-04 | 史金麟 | The method of one way of life rubbish deodorization and device thereof |
JP2017517384A (en) * | 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. | Apparatus and method for thermal contact treatment of material and pyrolysis oil produced thereby |
JP2018053197A (en) * | 2016-09-30 | 2018-04-05 | 東日本高速道路株式会社 | Thermal decomposition system and thermal decomposition method |
JP2018203828A (en) * | 2017-05-31 | 2018-12-27 | 日立造船株式会社 | Carbonization apparatus |
US10421919B2 (en) | 2014-07-03 | 2019-09-24 | Pyrocore S.A. | Gasifier |
CN112090920A (en) * | 2019-06-17 | 2020-12-18 | 藤森工业株式会社 | Raw material processing device |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR101315522B1 (en) * | 2012-09-19 | 2013-10-08 | 주식회사 유니바이오 | Method of manufacturering lowly absorbent powder fuel made from spent coffee bean |
CN103614151B (en) * | 2013-01-25 | 2015-11-25 | 农业部规划设计研究院 | Horizontal continuous charcoal carbonization device |
CN104099107B (en) * | 2014-03-05 | 2016-04-20 | 陆久余 | Sludge fuel makes equipment |
CN105174678B (en) * | 2015-08-31 | 2017-09-22 | 安徽卓新洁净能源科技有限公司 | Domestic sludge pyrolysis processing technique |
KR101825285B1 (en) * | 2016-03-21 | 2018-02-02 | 김성우 | Wide solid fuel burner |
CN108275858A (en) * | 2017-01-05 | 2018-07-13 | 昆山沿沪水务有限公司 | A kind of Treatment of Sludge carbonization system |
CN107755407B (en) * | 2017-08-09 | 2020-06-16 | 北京国电富通科技发展有限责任公司 | Harmless recycling treatment device and method for organic hazardous wastes |
WO2019085528A1 (en) * | 2017-11-03 | 2019-05-09 | 董平年 | Cracking and reduction conversion method for household organic wastes |
CN108180750B (en) * | 2017-12-25 | 2023-04-07 | 北矿磁材科技有限公司 | Drying kiln and method for auxiliary drying of chromium-containing material through drying kiln by utilizing hot waste gas |
JP7154925B2 (en) * | 2018-10-03 | 2022-10-18 | メタウォーター株式会社 | Screw separator and wastewater treatment system |
CN113019263B (en) * | 2019-12-25 | 2023-09-01 | 新疆硅基新材料创新中心有限公司 | SiO (silicon dioxide) X Thermal treatment method and system for @ C composite material |
CN111117675B (en) * | 2020-01-07 | 2021-03-19 | 山东理工大学 | Sectional spiral stirring type biomass pyrolysis liquefaction system |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH08245966A (en) * | 1995-03-13 | 1996-09-24 | Jun Fujiki | Treatment of waste by carbonization |
JPH11293258A (en) * | 1998-04-06 | 1999-10-26 | Nakata Giken:Kk | Carbonization oven |
JP2003213269A (en) * | 2002-01-28 | 2003-07-30 | Ebara Corp | High temperature carbonization installation and high temperature carbonization method |
JP2003292964A (en) * | 2002-04-02 | 2003-10-15 | Meidensha Corp | Apparatus and facility for heat treatment |
JP2004049973A (en) * | 2002-07-17 | 2004-02-19 | Meidensha Corp | Sludge treatment method and facilities therefor |
JP2005274018A (en) * | 2004-03-24 | 2005-10-06 | Meidensha Corp | Indirect heating working system and indirect heating working method |
JP2008106221A (en) * | 2006-09-29 | 2008-05-08 | Shinten Kogyo Kk | Carbonization apparatus |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP3539557B2 (en) * | 2001-03-09 | 2004-07-07 | 日生エンジニアリング株式会社 | Carbonization equipment and equipment |
-
2009
- 2009-10-16 CN CN2009801414815A patent/CN102186948A/en active Pending
- 2009-10-16 MY MYPI2011001714A patent/MY156263A/en unknown
- 2009-10-16 MY MYPI2015000616A patent/MY169929A/en unknown
- 2009-10-16 WO PCT/JP2009/067917 patent/WO2010047283A1/en active Application Filing
- 2009-10-16 JP JP2010534791A patent/JP5480814B2/en active Active
-
2013
- 2013-05-13 JP JP2013101618A patent/JP5632504B2/en active Active
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH08245966A (en) * | 1995-03-13 | 1996-09-24 | Jun Fujiki | Treatment of waste by carbonization |
JPH11293258A (en) * | 1998-04-06 | 1999-10-26 | Nakata Giken:Kk | Carbonization oven |
JP2003213269A (en) * | 2002-01-28 | 2003-07-30 | Ebara Corp | High temperature carbonization installation and high temperature carbonization method |
JP2003292964A (en) * | 2002-04-02 | 2003-10-15 | Meidensha Corp | Apparatus and facility for heat treatment |
JP2004049973A (en) * | 2002-07-17 | 2004-02-19 | Meidensha Corp | Sludge treatment method and facilities therefor |
JP2005274018A (en) * | 2004-03-24 | 2005-10-06 | Meidensha Corp | Indirect heating working system and indirect heating working method |
JP2008106221A (en) * | 2006-09-29 | 2008-05-08 | Shinten Kogyo Kk | Carbonization apparatus |
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2016093811A (en) * | 2010-02-02 | 2016-05-26 | 株式会社ガイア環境技術研究所 | Method for producing oil and gas adsorbent, and oil and gas adsorbent |
JP6002877B2 (en) * | 2010-02-02 | 2016-10-05 | 株式会社ガイア環境技術研究所 | Method for producing oil or gas adsorbent and oil or gas adsorbent |
JP2014500892A (en) * | 2010-10-26 | 2014-01-16 | 西峡龍成特種材料有限公司 | Heated gas circulation type carbon material decomposition method and equipment |
JP2012206011A (en) * | 2011-03-29 | 2012-10-25 | Gaia Kankyo Gijutsu Kenkyusho:Kk | Water purifying material and method for production thereof |
JP2013117524A (en) * | 2011-10-31 | 2013-06-13 | Gaia Institute Of Environmental Technology Inc | Method for manufacturing carbide which absorb and filter radioactive substance and method for using the same, and water purifier, water treatment apparatus and functional food |
JP2014121698A (en) * | 2012-11-22 | 2014-07-03 | Gaia Institute Of Environmental Technology Inc | Flocculation aid of porous charcoal, filtration aid of porous charcoal and water treatment method |
CN103834418B (en) * | 2014-04-02 | 2015-06-10 | 青岛伊诺威能源化工新技术有限公司 | Transverse alternate heating and vertical coke discharging type tamping coke furnace |
CN103834418A (en) * | 2014-04-02 | 2014-06-04 | 青岛伊诺威能源化工新技术有限公司 | Transverse alternate heating and vertical coke discharging type tamping coke furnace |
JP2017517384A (en) * | 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. | Apparatus and method for thermal contact treatment of material and pyrolysis oil produced thereby |
US10414987B2 (en) | 2014-04-15 | 2019-09-17 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. | System and method for thermocatalytic treatment of material and pyrolysis oil produced therewith |
GB2529053A (en) * | 2014-07-03 | 2016-02-10 | Dps Bristol Holdings Ltd | Waste processing apparatus |
US10421919B2 (en) | 2014-07-03 | 2019-09-24 | Pyrocore S.A. | Gasifier |
CN104258438A (en) * | 2014-10-16 | 2015-01-07 | 史金麟 | Method and device for deodorizing domestic waste |
CN104258438B (en) * | 2014-10-16 | 2017-01-04 | 史金麟 | The method of one way of life rubbish deodorization and device thereof |
JP2018053197A (en) * | 2016-09-30 | 2018-04-05 | 東日本高速道路株式会社 | Thermal decomposition system and thermal decomposition method |
JP2018203828A (en) * | 2017-05-31 | 2018-12-27 | 日立造船株式会社 | Carbonization apparatus |
CN112090920A (en) * | 2019-06-17 | 2020-12-18 | 藤森工业株式会社 | Raw material processing device |
Also Published As
Publication number | Publication date |
---|---|
JP5632504B2 (en) | 2014-11-26 |
CN102186948A (en) | 2011-09-14 |
JPWO2010047283A1 (en) | 2012-03-22 |
MY169929A (en) | 2019-06-17 |
JP2013177620A (en) | 2013-09-09 |
JP5480814B2 (en) | 2014-04-23 |
MY156263A (en) | 2016-01-29 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP5480814B2 (en) | Carbonization apparatus and carbonization method | |
JP2006274201A (en) | Continuous reduced-pressure drying/carbonizing apparatus | |
JP6431469B2 (en) | Method for producing oil or gas adsorbent and oil or gas adsorbent | |
JP6124494B1 (en) | Plant biomass semi-carbide production equipment | |
CN1358221A (en) | Dry-distilling/volume reducing device for wastes | |
JP2005146119A (en) | Method and apparatus for carbonizing organic waste material | |
JP3359307B2 (en) | Method and apparatus for drying and carbonizing organic waste | |
JP5176016B2 (en) | Superheated steam continuous recycling equipment | |
CN110295063B (en) | Biomass external heating method heat and carbon co-production system and method | |
JP4478441B2 (en) | Production facilities for dry matter and carbonized manure | |
JP2012224677A (en) | System and method for carbonizing wet biomass | |
CN110257093B (en) | Control method of carbonization system in biomass external heating method heat and carbon co-production system | |
CN105371280B (en) | The apparatus and method that a kind of solid waste organic substance cleaning is burned | |
CN103486594B (en) | Low temperature distillation processes the new technique of domestic waste in conjunction with high temperature fission | |
Orge et al. | Design improvement of the PhilRice continuous-type rice hull carbonizer for biochar production towards sustainable agriculture | |
WO2015087568A1 (en) | Poultry manure treatment method and poultry manure treatment system | |
KR101005850B1 (en) | Apparatus for Drying and Carbonating Combustibile or organic Waste | |
JP4077811B2 (en) | Heat treatment equipment using superheated steam | |
JP4295942B2 (en) | Production facilities for dry fertilizer made from livestock manure | |
JP2011068824A (en) | Carbonization facility for organic water-containing waste | |
JP5945929B2 (en) | Waste gasification and melting equipment | |
CA2723601C (en) | Method and apparatus for efficient production of activated carbon | |
WO2011014094A1 (en) | Method and device for recycling moist waste matter comprising organic materials | |
CN106765166B (en) | A kind of high temperature garbage burning processing equipment | |
CN206143142U (en) | System for handle domestic waste |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 200980141481.5 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 09821980 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2010534791 Country of ref document: JP Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 12011500779 Country of ref document: PH |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 09821980 Country of ref document: EP Kind code of ref document: A1 |