WO2010047283A1

WO2010047283A1 - Apparatus for carbonization and method of carbonization

Info

Publication number: WO2010047283A1
Application number: PCT/JP2009/067917
Authority: WO
Inventors: 信和田口
Original assignee: 合資会社Liberty Net INTERNATIONAL
Priority date: 2008-10-20
Filing date: 2009-10-16
Publication date: 2010-04-29
Also published as: JP5632504B2; CN102186948A; JPWO2010047283A1; MY169929A; JP2013177620A; JP5480814B2; MY156263A

Abstract

A system for reduction and carbonization is provided, in which a wide range of raw materials can be used to produce regenerated carbon having a high energy. The system is a carbonization apparatus in which an organic substance is dried and pyrolyzed in a kiln (2) and heat is stored in the same kiln. The apparatus is characterized by comprising a rotatable kiln (2) having an inlet and an outlet, a raw-material feeder for introducing an organic substance into the kiln (2) through the inlet, and a combustion chamber (3) which has the kiln (2) in the inner space thereof and supplies heat to the kiln (2) from outside, and by being configured so that an organic substance having a high water content resides in the kiln (2) for a longer time period than an organic substance having a low water content. The apparatus is further characterized in that the kiln (2) has, on the inner circumferential surface, a spiral blade (1a) spirally extending in the length direction for the kiln (2) and one or more stirring blades (1b) projecting inward.

Description

Carbonization apparatus and carbonization method

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. Thus, 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.

JP 2001-322809 A

Conventionally, 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. Is provided with a raw material supply device, and an activated carbide discharge device is provided at the end outlet of the carbonization tube. 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. There is known 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). ).

In addition, 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. In this case, the atmosphere gas is reduced or a low oxygen atmosphere as a condition for detoxifying (dechlorinating) the ash (dioxin decomposition condition).

However, in 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.

Therefore, in view of the above circumstances, 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.

According to the reduction carbonization processing system according to claim 1, 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.

According to the reduction carbonization processing system according to claim 5, 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.

According to a sixth aspect of the present invention, 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. The reduction carbonization apparatus according to claim 1, further comprising: a deodorization unit that deodorizes odorous gas.

According to the reduction carbonization processing system according to claim 6, by separating the water vapor generated inside the kiln into odor gas and water by cooling the water vapor generated inside the kiln by a 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.

According to the reduction carbonization processing system of claim 7, 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.

According to the reduction carbonization processing system of claim 8, 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. An apparatus for reducing carbonization according to any one of claims 1 to 8, further comprising an oiling section that converts to oil.

According to the reduction carbonization processing system according to claim 9, 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.

According to a tenth aspect of the present invention, 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.

According to the reduction carbonization processing system of claim 10, 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.

According to the reduction carbonization processing method according to claim 11, 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 carbonization method according to

claim

12 or 13.

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 carbonization method according to 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.). In general, it is considered that air is supplied in a state where the whole meets or exceeds the self-ignition temperature and the dry distillation gas starts to burn. However, 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. Therefore, it is possible to continue high-temperature combustion without supplying heat from the heating source 9. Accordingly, it is possible to realize a carbonization process that does not require energy from the outside. An amount of air sufficient to cause self-combustion is contained in the raw material and that air is also introduced into the recovery chamber. In addition, oxygen generated by pyrolysis of organic matter in the kiln is also led to the recovery chamber.

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 (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 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.
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 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. It is.

The carbonization processing system of the present invention can generate high energy regenerated coal using a wide range of raw materials.

It is explanatory drawing of the carbonization processing system which concerns on one Embodiment of this invention. It is a system block diagram of the carbonization processing system concerning one embodiment of the present invention. It is a system block diagram of the pretreatment process in the carbonization processing system concerning one embodiment of the present invention. It is a conceptual diagram which shows the process in the carbonization processing system which concerns on embodiment of this invention. It is the side surface conceptual diagram and longitudinal direction vertical sectional view which show the other structure for adjusting the residence time of organic substance. It is a conceptual diagram for demonstrating the effect | action of the structure shown in FIG. It is a microscope picture of regenerated charcoal (coffee bean dregs charcoal). It is a microscope picture of regenerated charcoal (plum seed charcoal). It is a microscope picture of regenerated charcoal (okara charcoal). It is a microscope picture of regenerated charcoal (cow dung charcoal). It is a microscope picture of regenerated charcoal (pig dung charcoal). It is a microscope picture of regenerated charcoal (sludge charcoal). It is a microscope picture of regenerated charcoal (rice husk charcoal). It is a conceptual sectional view showing a carbonization device concerning other embodiments.

DESCRIPTION OF SYMBOLS 1a ... Spiral blade 1b Stirring blade 2 ... Kiln 2a Drying part 2b Carbonization part 2d Heat storage part 2c Internal space 2in Inlet 2out Outlet 3 ... Combustion chamber 3a ... Exhaust pipe 4 ... Heat source 5 ... Piping part 6 ... Cooling part 7 ... Deodorizing Part 8: Dry distillation gas recovery part 9 ... Auxiliary heating source 10 ... Steam smoke path 11 ... Oil generation part 12 ... Water distribution pipe 13 ... Fan 14 ... Hopper 15 ... Raw material supply pipe 16 ... Supply screw 17 ... Second discharge pipe 18 ... Cooling Apparatus 19 ... Connection pipe 20 ... Conveying screw 21 ... Conveying screw 22 ... Vapor vent pipe 23 Chimney part 24 Circulation pipe 25 Gas vent pipe 30 Connection part 60 Recovery part

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.

(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.

As shown in FIG. 1, a reduction carbonization apparatus 1 applied to a reduction carbonization system according to an embodiment of the present invention 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 according to an embodiment of the present invention 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. A recovery unit 6 for temporarily retaining the recovered rice husk charcoal Q so as to prevent intrusion.

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. Thereby, the rice husk P stored in the hopper 14 is supplied to the internal space 2 c by the conveyance of the supply screw 16.

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. As a result, 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. Thereby, 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 (not shown) 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. At this time, 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.

Specifically, 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. A first discharge pipe 18, a second discharge pipe 17 piped in the same direction as the axial direction of the kiln 2 below the downstream end of the first discharge pipe 18, a conveying screw 20 provided in the

discharge pipes

17, 18, 21, the rice husk charcoal Q conveyed by the conveying

screws

20, 21 blocks the internal space 2 c of the kiln 2 from the outside (atmosphere).

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. Further, 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. Further, the 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.

As a result, 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.

As shown in FIG. 1 and FIG. 2, a reduction carbonization processing apparatus according to an embodiment of the present invention 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.

5 and 6, 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. In the internal space 2c,

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. . At this time, 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 longer it goes to the side. In addition, 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. In this step, 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. In this step, 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.

Further, 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.

As shown in FIG. 1, FIG. 4 or FIG. 5, when the drying process, carbonization (pyrolysis) process, and heat storage process are carried out in one kiln, the upper part is steam, the lower part is dry distillation gas, the bottom part is Carbide is present.

As shown in FIG. 4, for example, when two pipes are connected vertically on the downstream side of the pipe section 5 shown in FIG. 1, due to the difference in gravity, the lower piping is subjected to the dry distillation gas flow, the upper pipe Water vapor and odorous gas flow through.

In this case, 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.

According to such a configuration, the water vapor generated inside the kiln 2 using the difference in specific gravity by the two or three pipe portions 5 and the gas having a lighter specific gravity or a higher specific gravity than the water vapor. By separating, hydrogen gas lighter than water vapor, carbon monoxide, methane gas, hydrocarbon gas, etc. heavier than water vapor can be separated from water vapor.

Moreover, the cooling part 6 which isolate | separates the water vapor | steam which generate | occur | produced inside the kiln 2 into the odor gas and water by cooling the water vapor | steam generated inside the kiln 2, and the odor gas separated by being connected to the cooling part 6 is separated. And a deodorizing unit 7 for deodorizing.

According to such a configuration, 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.

In addition, 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.

According to such a configuration, 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.

Also, 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.

According to such a configuration, 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.

Moreover, the vapor | steam path | route 10 which collect | recovers the smoke which generate | occur | produced in the carbonization initial stage of the organic substance etc. in the vicinity of the termination | terminus part of the drying part 2a or the carbonization part 2b, and the liquefaction which oilizes by cooling the collected smoke Part 11.

According to such a configuration, after the smoke generated at the initial stage of carbonization of the organic matter or the like in the vicinity of the end portion of the drying unit 2a or the start end portion of the carbonization unit 2b is collected by the vapor smoke path 10, the oily unit 11 collects the smoke. Smoke can be cooled and oiled to produce recycled oil.

Furthermore, 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. Features.

According to such a configuration, 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.

For example, 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.

In this example, 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 | disassembly part C from the drying part B. FIG.

A plurality of stirring blades 1b may be provided. In the example shown in FIG. Moreover, it is preferable to incline the line connected to the center. This inclination may be appropriately changed depending on the water content of the organic matter. In the example shown in FIG. 5, an inclination of 60 ° is provided in the counterclockwise direction with reference to the line connecting the center. Moreover, it is preferable that 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.

As shown in FIG. 6, when the kiln rotates, the organic matter is lifted up by the stirring blades 1b provided on the inner circumferential surface. An organic substance having a high water content is an organic substance having a high adhesiveness, and an organic substance having a low water content is an organic substance having a low adhesiveness.

Therefore, an organic substance having a high water content is lifted to a higher position than an organic substance having a low water content. FIG. 6A shows the case where the water content is high, and FIG. 6B shows the case where the water content is low. In the case of FIG. 6A, the organic matter falls after being lifted to a high position. On the other hand, in the case of FIG. 6B, the organic substance falls at a low position. When falling from a high position, many organic substances return to the back as shown in FIG. As a result, the time spent in the drying process becomes longer. On the other hand, when falling from a low position, few organic substances return to the back. As a result, the time spent in the drying process is shortened.

In this structure, 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.

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 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.
Further, 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. Provided a flow line,
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 kiln 2, the volume of water vapor becomes a problem. Under atmospheric pressure, 1 liter of water is 100. With C, the volume of water vapor is about 1,700 liters. Also 373. In C, the volume of water vapor is about 3,400 liters.
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.
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 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.

(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 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.

For example, 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. . At this time, 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.

Specifically, 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. In addition, it is preferable to arrange the conveying screw 21 also inside the discharge pipe 17.

On the other hand, 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.

At this time, since the inside of the kiln 2 is indirectly heated in a reduced state in an oxygen-free atmosphere, self-combustion accompanied by indirect thermal decomposition of organic matter or the like occurs (self-ignition at 225 to 500 ° C.). Thereafter, the heating of the heating source 4 is stopped.

Thereby, the dry distillation gas recovered from the inside of the kiln 2 is basically in a high temperature environment. For example, depending on the detection result of a sensor or the like (not shown) that monitors the internal temperature of the kiln 2, 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). In addition, you may use the heating of the heating source 4 together.

In addition, 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. When 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.

Then, when 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.

In addition, 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.

Also, 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. If necessary (for example, depending on the type of organic matter P, etc.), 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 (combustion) 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.

Therefore, by performing this emulsion combustion, 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.

In addition, in emulsion combustion, 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.

By the way, as the organic matter P in the present invention, 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.

Moreover, in the kiln 2, a high temperature environment of 850 ° C. could be realized, and combustion could be completed in a residence time of 2 seconds or more.

In addition, 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).

In the reduction carbonization processing system of the present invention, for example, as shown in Table 1, by changing the length and number of kilns 2, 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. When the inner diameter of the kiln 2 is 500φ, 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

In order to confirm these various conditions, it is preferable to use 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.

Then, various recovered charcoal collected was examined.

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 (water content 80%), fuel calorific value is 5440 Kcal / kg per kg (fixed carbon rate 78.5%)
Raw material: When rice husk (water content 2%) is carbonized (15 minutes), the calorific value of fuel is 4544 Kcal / kg per kg (fixed carbon rate 46.6%, silica 41.6%)
All were able to produce regenerated coal with high energy. The test was conducted according to JIS-Z 7302-2.

For reference, the calorific value of coal (coke) is 7,190 Kcal / kg, and the calorific value of wood is 3,440 Kcal / kg.

As described above, according to the reduction carbonization processing system of the present invention, 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.

The micrographs of the above regenerated coal are shown in FIGS.

In all examples, the porous state and the fibrous state are shown, indicating that the carbonization was performed extremely well.

As described above, according to the present invention, it is possible to provide a reductive carbonization system capable of generating high energy regenerated coal using a wide range of raw materials.

Claims

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.
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.
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.
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.
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.
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:
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.
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.
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.
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.
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.
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.
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.
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.
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.
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.
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.
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.
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. .