T e c h n i c a l F i e l d
The present invention relates to a pyrolysis
apparatus for continuously pyrolyzing a solid organic
material by heating the material, while causing the
5 material to flow.
Background A r t
When a solid organic material is continuously
pyrolyzed by heating the material, while causing the
material to flow, a rotary kiln described in Patent
10 Literature 1 listed below can be used, for example. The
rotary kiln described in Patent Literature 1 is
configured as follows. Specifically, an organicmaterial
(material to be treated) is suppliedto an inner cylinder
(furnace core tube), and the inner cylinder is rotated.
15 While the organic material is caused to flow in the inner
cylinder by the rotation, the organic material is heated
by introducing heated gas into anouter cylinder (heating
furnace). In this manner the organic material can be
continuously pyrolyzed. In addition, the measurement of
20 the temperature of the organic material with a
thermocouple provided to the inner cylinder makes it
possible to adjust the temperature of the heated gas.
C i t a t i o n L i s t
P a t e n t L i % e r a t u r e
25 Patent Literature 1: Japanese Patent Application
Publication No. 2000-292068
Summary of Invention
Technical Problem
However, in the rotary kiln described in Patent
Literature 1 mentioned above, the temperature of the
5 organic material in contact with the thermocouple is
considered to be the temperature of the entire organic
material. Hence, when the temperature of the organic
material in contact with the thermocouple is very
different from the average temperature of the entire
PO organic material, the entire organic material is not
heated with a necessary and sufficient amount of heat,
andit is possiblethatthe entire organicmaterial cannot
be pyrolyzed with a desired pyrolysis ratio (degree).
In view of this, an object of the present invention
15 is to provide a pyrolysis apparatus capable ofpyrolyzing
the entire organic material with a desired pyrolysis
ratio and with high precision.
Solution to Problem
To solve the above-described problem, a pyrolysis
20 apparatus according to a first aspect of the invention
is characterized in that
the pyrolysis apparatus comprises:
a furnacemainbody in which a solid organicmaterial
flows;
25 organic material supply means for supplying the
organic material into the furnace main body;
heating means for heating the organic material in
the furnace main body;
s e n d i n g - o u t means f o r s e n d i n g o u t a s o l i d p y r o l y s i s
p r o d u c t a n d a p y r o l y s i s g a s r e s u l t i n g from t h e h e a t i n g
and p y r o l y s i s i n t h e f u r n a c e main body;
s t a n d a r d g a s s u p p l y means f o r a d d i n g a s t a n d a r d g a s
5 i n c l u d i n g a n i n e r t g a s t o t h e p y r o l y s i s g a s ;
g a s c o n c e n t r a t i o n m e a s u r e m e n t means f o r m e a s u r i n g
a c o n c e n t r a t i o n c s o f t h e s t a n d a r d g a s a n d a c o n c e n t r a t i o n
C c o f a n a n a l y t e g a s i n c l u d i n g a t l e a s t o n e o f c a r b o n
monoxide, c a r b o n d i o x i d e , h y d r o g e n g a s , h y d r o c a r b o n
10 g a s e s , and H20 i n a m i x t u r e g a s o f t h e p y r o l y s i s g a s and
t h e s t a n d a r d g a s s e n t o u t of t h e s e n d i n g - o u t means; and
a r i t h m e t i c c o n t r o l means f o r
c a l c u l a t i n g a n a m o u n t F c o f t h e a n a l y t e g a s g e n e r a t e d
p e r u n i t w e i g h t o f t h e o r g a n i c m a t e r i a l by t h e f o l l o w i n g
15 f o r m u l a (1) on t h e b a s i s o f t h e c o n c e n t r a t i o n C c o f t h e
a n a l y t e g a s a n d t h e c o n c e n t r a t i o n C s o f t h e s t a n d a r d g a s
m e a s u r e d by t h e g a s c o n c e n t r a t i o n m e a s u r e m e n t means, a
f l o w amount Fs p e r u n i t t i m e o f t h e s t a n d a r d g a s a d d e d
from t h e s t a n d a r d g a s s u p p l y means, and a w e i g h t Wo o f
20 t h e o r g a n i c m a t e r i a l s u p p l i e d p e r u n i t t i m e from t h e
o r g a n i c m a t e r i a l s u p p l y m e a n s i n t o t h e f u r n a c e m a i n b o d y ,
d e t e r m i n i n g a p y r o l y s i s r a t i o D t p e r u n i t w e i g h t o f
t h e o r g a n i c m a t e r i a l f r o m a map b e i n g i n p u t t e d i n a d v a n c e
and s h o w i n g a r e l a t i o n s h i p b e t w e e n t h e amount Fc o f t h e
25 a n a l y t e g a s g e n e r a t e d a n d a p y r o l y s i s r a t i o p e r u n i t
w e i g h t o f t h e o r g a n i c m a t e r i a l , and
c o n t r o l l i n g t h e h e a t i n g means t o make t h e p y r o l y s i s
r a t i o D t e q u a l t o a d e s i r e d p y r o l y s i s r a t i o D r :
Fc={ Fs ( C c / C s ) } /Wo (1) e
30 Meanwhile, a p y r o l y s i s a p p a r a t u s a c c o r d i n g t o a
s e c o n d a s p e c t o f t h e i n v e n t i o n i s t h e p y r o l y s i s a p p a r a t u s
according to the first aspect of the invention,
characterized in that
the arithmetic control means controls the heating
means to raise a heating temperature of the organic
5 material, when the pyrolysis ratio Dt is lower than the
pyrolysis ratio Dr.
Meanwhile, a pyrolysis apparatus according to a
third aspect of the invention is the pyrolysis apparatus
according tothe first or second aspect ofthe invention,
10 characterized in that
the arithmetic control means controls the heating
means to lower a heating temperature of the organic
material, when the pyrolysis ratio Dt is higher than the
pyrolysis ratio Dr.
15 Meanwhile, a pyrolysis apparatus according to a
fourth aspect ofthe invention is the pyrolysis apparatus
according to any one of the first to third aspects of
the invention, characterized in that
the heating means heats the furnace main body from
20 outside.
Meanwhile, a pyrolysis apparatus according to a
fifth aspect of the invention is the pyrolysis apparatus
according to any one of the first to fourth aspects of
the invention, characterized in that
25 the standard gas supply means supplies the standard
gas to the furnace main body on an upstream side thereof
in a flow direction of the - organic material,
Meanwhile, a pyrolysis apparatus according to a
sixth aspect of the invention is the pyrolysis apparatus
30 according to any one of the first to fifth aspects of
the invention, characterized in that
the organic material is a low-rank coal.
Advantageous Effects of Invention
In the pyrolysis apparatus according to the present
invention, the arithmetic control means calculates the
5 generated amount Fc of the analyte gas by the
above-described formula (1) on the basis of the
concentrationCc ofthe analyte gas and the concentration
Cs of the standard gas, as well as the flow amount Fs
of the standard gas and the weight Wo of the organic
10 material, determines the pyrolysis ratio Dt of the
organic material from the map being inputted in advance
and showing the relationship between the generated
amount Fc of the analyte gas and the pyrolysis ratio of
the organic material, and controls the heating means to
15 make the pyrolysis ratio Dt equal to a desired pyrolysis
ratio Dr. Hence, the amount of heatappliedtothe organic
material can be set on the basis of the pyrolysis ratio
(degree) of the entire organic material after the
completion of pyrolysis. Therefore, even when the
20 temperature of the organic material in the furnace main
bodygreatlyvaries depending on the position, the entire
organic material can be heated with a necessary and
sufficient amount of heat without being influenced by
the variation. Consequently, the entire organicmaterial
25 can be pyrolyzed with a desired pyrolysis ratio Dr and
with high precision.
Brief Description of Drawings
Fig. 1 is a schematic structural diagram of a main
embodiment of a pyrolysis apparatus according to the
present invention.
5 Fig. 2 is a map showing a relationship between the
amount of carbon dioxide generated per unit weight of
low-rank coal and the pyrolysis ratio (degree) of the
low-rank coal for each type of low-rank coal and being
inputted in advance into an arithmetic control device
PO of the pyrolysis apparatus of Fig. 1.
Fig. 3 is a map showing a relationship between the
amount of carbon monoxide generated per unit weight of
low-rank coal and the pyrolysis ratio (degree) of the
low-rank coal for each type of low-rank coal and being
1% inputted in advance into arithmetic control means of
another embodiment of the pyrolysis apparatus according
to the present invention.
Fig. 4 is a map showing a relationship between the
amount of methane (a hydrocarbon gas) generated per unit
20 weight of low-rank coal and the pyrolysis ratio (degree)
of the low-rank coal for each type of low-rank coal and
being inputted in advance into arithmetic control means
of still another embodiment of the pyrolysis apparatus
according to the present invention.
25 Description of Embodiments
Embodiments of a pyrolysis apparatus according to
the present invention are described based on the
drawings; however, the present invention is not limited
exclusivelytothe following embodiments describedbased
on the drawings.
A main embodiment of the pyrolysis apparatus
5 according to the present invention is described based
on Figs. 1 and 2.
As shown in Fig. 1, in a fixedly supported outer
cylinder (jacket) 111, an inner cylinder (furnace main
body) 112 is rotatably supported. To a base end (on the
10 left side in Fig. 1) of the inner cylinder 112, a tip
end (on the right side in Fig. 1) of a supply feeder 113
is connected, while allowing the rotation of the inner
cylinder112. The supply feeder113 feeds adriedlow-rank
coal (low-quality coal) 1 such as lignite or
15 sub-bituminous coal, which is a solid organic material,
On a base end side (the left side in Fig. 1) of the
supply feeder 113, a supply hopper 114 into which the
low-rank coal 1 can be introduced is provided. On a base
end side of the inner cylinder 112, a standard gas supply
20 source 115 which is standard gas supply means for
supplying a standard gas 4 including nitrogen gas is
connected to the inner cylinder 112, with a flow amount
adjustment valve 115a provided therebetween.
On the tip end side (the right side in Fig. 1) of
25 the inner cylinder 112, a chute 116 is connected to the
inner cylinder 112, while allowing the rotation of the
inner cylinder 112. The chute 116 is sending-out means
for dropping downward and sending out pyrolyzed coal 2,
which is a solid pyrolysis productobtainedbypyrolyzing
30 the low-rank coal 1, and for sending out pyrolysis gas
3, formed with the progress of the pyrolysis of the
low-rank coal 1, through an upper portion of the chute
116. The upper portion of the chute 116 is connected to
a combustion furnace 117 where the pyrolysis gas 3 is
5 combusted.
To the combustion furnace 117, a fuel supply source
118 for supplying a fuel 5 for combustion such as natural
gas into the combustion furnace 117 is connected, with
a flow amount adjustment valve 118a provided
10 therebetween. In addition, an air blower 119 for
supplying air 6 for combustion into the combustion
furnace 117 is connected to the combustion furnace 117.
The combustion furnace 117 is configured such that
combustion gas 7 can be generated by combustion of the
15 pyrolysis gas 3 with the fuel 5 and the air 6 and sent
out.
An outlet for the combustion gas 7 of the combustion
furnace 117 is connected to the inside of the outer
cylinder 111, To the outer cylinder 111, an exhaust line
20 llla is connected through which the combustion gas 7 fed
into the outer cylinder 111 is emitted to the outside
of the system.
A portion between the upper portion of the chute 116
and the combustion furnace 117 is connected to a gas
25 concentration measurement device 131 such as a gas
chromatograph. The gas concentration measurement device
131 is gas concentration measurement means for taking
out an aliquot of a mixture gas of the pyrolysis gas 3
and the standard gas 4 sent out of the chute 116, and
30 measuring the concentrations of components in the gas.
The gas concentration measurement device 131 is
electrically connected to an input unit of an arithmetic
control device 130, which is arithmetic control means.
An output unit of the arithmetic control device 130
is electrically connected to a driving motor 113a of the
5 supply feeder 113, the flow amount adjustment valve 115a
of the standard gas supply source 115, the flow amount
adjustment valve 118a of the fuel supply source 118, and
the air blower 119. The arithmetic control device 130
is configured such that the arithmetic control device
10 130 can control operations of the driving motor 113a,
the flow amount adjustment valves 115a and 118a, the air
blower 119, and the like on the basis of information from
the gas concentration measurement device 131,
information inputted in advance, and the like (details
15 are described later).
Note that, in this embodiment, organic material
supply means is constituted by the supply feeder 113,
the supply hopper 114, and the like, and heating means
is constituted by the outer cylinder 111, the combustion
20 furnace 117, the fuel supply source 118, the air blower
119, and the like.
Next, operations of such a pyrolysis apparatus 100
according to this embodiment are described.
After introduction of the low-rank coal 1. into the
25 supply hopper 114, the type of the low-rank coal I, a
desired pyrolysis ratio (degree) Dr of the low-rank coal
1, a weight Wo of the low-rank coal 1 supplied per unit
time into the inner cylinder 112, and a flow amount Fs
per unit time of the standard gas 4 supplied into the
30 inner cylinder 112 are inputtedtothe arithmetic control
device 130, and the inner cylinder 112 is rotated. Here,
the arithmetic control device 130 controls an operation
of the driving motor 113a of the supply feeder 113 to
supply the low-rank coal 1 into the inner cylinder 112
at the inputtedweightwoper unit time, and also controls
5 an operation of the flow amount adjustment valve 115a
of the standard gas supply source 115 to supply the
standard gas 4 into the inner cylinder 112 at the inputted
flow amount Fs per unit time. Meanwhile, the arithmetic
control device 130 controls operations ofthe flow amount
10 adjustment valve 118a of the fuel supply source 118 and
the air blower 119 to feed the fuel 5 and the air 6 at
standard flow amounts forthe beginning ofthe operations,
so that combustion gas 7 is generated at a standard
temperature in the combustion furnace 117 and fed into
3.5 the outer cylinder 111.
With the rotation of the inner cylinder 112, the
low-rankcoal 1 s u p p l i e d i n t o t h e i n n e r c y l i n d e r 1 1 2 m o v e s
in a flowing manner from the base end side (the left side
in Fig. 1) to the tip end side (the right side in Fig.
20 1) of the inner cylinder 112, while being stirred,
Simultaneously, the low-rank coal 1 is heated indirectly
through the inner cylinder 112 by the combustion gas 7
fed into the outer cylinder 111, and pyrolyzed into
pyrolyzed coal 2, which is sent out to the chute 116,
25 and sent out to the outside of the system through the
lower portion of the chute 116.
Note that the combustion gas 7 having heated the
inner cylinder 112 is emittedtothe outside ofthe system
through the exhaust line llla.
30 In addition, the pyrolysis gas 3 generated with the
heating and pyrolysis of the low-rank coal 1 is sent out
to the chute 116, while being mixed in the inner cylinder
112 with the standard gas 4 supplied from the standard
gas supply source 115 into the inner cylinder 112 on an
upstream side thereof in a flow direction ofthe low-rank
5 coal 1 to form a mixture gas with the standard gas 4.
The mixture gas is sent out through the upper portion
of the chute 116. While an aliquot of the mixture gas
is taken out to the gas concentration measurement device
131, the rest is fed into the combustion furnace 117,
10 and combusted with the fuel 5 and the air 6 to form the
combustion gas 7, which is then fed into the outer
cylinder 111.
The gas concentration measurement device 131
measures constituent ratios (concentrations) of the
15 standard gas 4 and carbon dioxide which is an analyte
gas in the mixture gas taken out, and transmits the
information to the arithmetic control device 130.
The arithmetic control device 130 calculates an
amount (volume) Fc of carbon dioxide generated per unit
20 weight of the low-rank coal 1 by the following formula
(1) on the basis of the weight Wo of the low-rank coal
1 supplied per unit time into the inner cylinder 112 and
the flow amount Fs per unit time of the standard gas 4
supplied into the inner cylinder 112, which are
25 previously inputted, as well as the information from the
gas concentration measurement device 131, i. e., a
constituent ratio (concentration) Cc of carbon dioxide
in the mixture gas and a constituent ratio
(concentration) Cs of the standard gas 4 in the mixture
30 gas.
FC={FS (CC/CS) j /WO (1)
Subsequently, the arithmetic control device 130
determines apyrolysis ratio (degree) Dtofthepyrolyzed
coal2 corresponding tothe generated amount Fc of carbon
dioxide forthe previously inputtedtype of the low-rank
5 coal 1 from a map (see Fig. 2) showing a relationship
between the amount (volume) Fc of carbon dioxide
generated per unit weight of the low-rank coal 1 and the
loss (in weight) on pyrolysis per unit weight of the
low-rank coal 1, which are inputted in advance, i.e.,
10 the pyrolysis ratio (degree) Dt of the pyrolyzed coal
2.
Then, the arithmetic control device 130 compares the
pyrolysis ratio (degree) Dt of the pyrolyzed coal 2 with
the previouslyinputteddesiredpyrolysis ratio (degree)
15 Dr. When the pyrolysis ratio (degree) Dt takes a value
within the range of an allowable error of the pyrolysis
ratio (degree) Dr, the arithmetic control device 130
determines that the low-rank coal 1 is pyrolyzed with
the desired pyrolysis ratio (degree) Dr and controls an
20 operation of the flow amount adjustment valve 118a of
the fuel supply source 118 to feed the fuel 5 at the
current flow amount,
On the other hand, when the pyrolysis ratio (degree)
Dt takes a value which is not within the range of the
25 allowable error of the pyrolysis ratio (degree) Dr, and
which is smaller than the pyrolysis ratio (degree) Dr
(DtDr), the arithmetic control device 130 determines
that the loss (in weight) on pyrolysis per unit weight
PO ofthe low-rank coallis large, i.e., the pyrolysis ratio
(degree) of the pyrolyzed coal 2 is high, and controls
an operation of the flow amount adjustment valve 118a
of the fuel supply source 118 so that the fuel 5 can be
fed at a flow amount lower than the current flow amount
15 to lower the temperature of the combustion gas 7,
This enables the pyrolysis with the pyrolyzed coal
2 always having the desired ratio (degree) Dr.
In other words, the pyrolysis apparatus 100
according to this embodiment is configured as follows.
20 Specifically, by detecting the concentration of carbon
dioxide (analyte gas) in the pyrolysis gas 3 after the
completion of pyrolysis sent out through the chute 116
together with the pyrolyzed coal 2 after the pyrolysis,
the pyrolysis ratio (degree) of the pyrolyzed coal 2 is
25 determined from the map showing the relationship which
is determined in advance, and the temperature of the
combustion gas 7 is adjusted,
For this reason, in the pyrolysis apparatus 100
according to this embodiment, the amount of heat applied
30 to the low-rank coal 1 can be set on the basis of the
pyrolysis ratio (degree) of the entire pyrolyzed coal
2 after the completion of pyrolysis. Hence, even when
the temperature of the low-rank coal 1 in the inner
cylinder 112 greatly varies depending on the position,
the entire low-rank coal 1 can be heated with a necessary
5 and sufficient amount of heat without being influenced
by the variation.
Accordingly, the pyrolysis apparatus 100 according
to this embodiment makes it possible to pyrolyze the
entire low-rank coal 1 with the desired pyrolysis ratio
10 Dr and with high precision.
Moreover, the standard gas 4 is supplied to the
pyrolysis gas 3, and the generated amount of carbon
dioxide is determined on the basis of the ratio of carbon
dioxide in the pyrolysis gas 3 to the standard gas 4.
15 Hence, the amount of carbon dioxide generated can be
calculated with higher precision, and the entire
low-rank coal 1 can be pyrolyzed with the desired
pyrolysis ratio Dr and with high precision more reliably
in this case than, for example, in a case where the
20 generated amount of carbon dioxide is determined on the
basis of the flow amount of the pyrolysis gas 3 sent out
through the chute 116.
This is because, if the flow amount of the pyrolysis
gas 3 is measured by providing a flow meter or the like
25 between the chute 116 and the gas concentration
measurement device 131, tar components and the like
contained in the pyrolysis gas 3 adhere to the flow meter
or the like, sothatittendstobe difficult to accurately
measure the flow amount of the pyrolysis gas 3.
30
Note that, in the above-described embodiment, the
standard gas supply source 115 is connected on the base
end side of the inner cylinder 112, i.e., the upstream
5 side in the flow directionofthelow-rankcoallto supply
the standard gas 4 into the inner cylinder 112.
Alternatively, as another embodiment, it is also
possibleto, for example, connect the standardgas supply
source 115 to a position between the chute 116 and the
10 gas concentration measurement device 131 and supply the
standard gas 4 to the pyrolysis gas 3.
However, it is very preferable to connect the
standard gas supply source 115 on the base end side of
the inner cylinder 112, i.e., the upstream side in the
15 flow direction of the low-rank coal 1 and supply the
standard gas 4 into the inner cylinder 112 as in the case
ofthe above-described embodiment, because the pyrolysis
gas 3 and the standard gas 4 can be uniformlymixed easily
and reliably,
20 In addition, in the above-described embodiment, the
case of the pyrolysis apparatus 100 of a rotary kiln type
in which the inner cylinder 112 is rotatably supported
in the fixedly supported outer cylinder 111 is described.
Alternatively, as another embodiment, it is also
25 possible, for example, to use a pyrolysis apparatus of
a conveyor type in which an outer periphery of an inner
cylinder (furnace main body) is covered with an outer
cylinder (jacket), and a mesh conveyor or the like is
disposed in the inner cylinder.
In addition, in the above-described embodiment, the
pyrolysis is conducted by heating the low-rank coal 1
in the inner cylinder 112 with the combustion gas 7.
Alternatively, as another embodiment, it is also
5 possible, for example, to pyrolyze the low-rank coal 1
in the inner cylinder 112 by heating the inner cylinder
112 with an electric heater or the like.
However, it is very preferable to conduct the
pyrolysis by heating the low-rank coal 1 in the inner
10 cylinder 112 with the combustion gas 7 as in the case
ofthe above-described embodiment, because the pyrolysis
gas 3 generated with the pyrolysis of the low-rank coal
1 can be used as a raw material of the combustion gas
7 to achieve effective utilization.
15 In addition, in the above-described embodiment, the
combustion gas 7 is fed into the outer cylinder 111, and
the pyrolysis is conducted by heating the low-rank coal
1 indirectly through the inner cylinder 112.
Alternatively, as another embodiment, it is also
20 possible to, for example, heat the standard gas 4 by
passing the combustion gas 7 through a heat exchanger
and also passing the standard gas 4 through the heat
exchanger, supplytheheated standardgas 4 into the inner
cylinder 112, and conduct the pyrolysis by directly
25 heating the low-rank coal 1.
However, it is not very preferable to heat the
standard gas 4, supply the heated standard gas 4 into
the inner cylinder 112, and conduct the pyrolysis by
directly heating the low-rank coal 1, because a large
30 amount of the standard gas 4 has to be used, and the cost
increases.
In addition, in the above-described embodiment,
carbon dioxide in the pyrolysis gas 3 is employed as the
analyte gas. Alternatively, as another embodiment, it
is also possible to, for example, employ carbon monoxide
5 in the pyrolysis gas 3 as the analyte gas, and determine
a pyrolysis ratio (degree) Dt of the pyrolyzed coal 2
corresponding to the generated amount Fc of carbon
monoxide forthepreviouslyinputtedtype ofthe low-rank
coal 1 from a map showing a relationship between the
10 amount (volume) Fc of carbon monoxide generated per unit
weight of the low-rank coal 1 and the loss (in weight)
on pyrolysis per unitweightofthelow-rank coal1, i.e.,
the pyrolysis ratio (degree) Dt of the pyrolyzed coal
2 as shown in Fig. 3, and it is also possible to employ
15 methane (hydrocarbon gas) in the pyrolysis gas 3 as the
analyte gas, and determine a pyrolysis ratio (degree)
Dt ofthe pyrolyzed coal2 corresponding tothe generated
amount Fc of methane (hydrocarbon gas) forthe previously
inputted type of the low-rank coal 1 from a map showing
20 a relationship between the amount (volume) Fc of methane
(hydrocarbon gas) generated per unit weight of the
low-rank coal 1 and the loss (in weight) on pyrolysis
per unit weight of the low-rank coal 1, i.e., the
pyrolysis ratio (degree) Dt of the pyrolyzed coal 2, as
25 shown in Fig. 4.
Further, it is possible to employ hydrogen gas in
the pyrolysis gas 3 as the analyte gas or H20 in the
pyrolysis gas 3 as the analyte gas. An analyte gas of
a suitable type for the value of the desired pyrolysis
30 ratio Dt may be selected, as appropriate, considering
relational characteristics shown by a map determined in
advance.
Here, if necessary, it is also possible to select
multiple analyte gases and use a combination thereof.
5 In addition, in the above-described embodiment, the
case where nitrogen gas is used as the standard gas 4
is described. Alternatively, as another embodiment, for
example, an inert gas such as helium gas or argon gas
can be used as the standard gas 4.
10 However, it is very preferable to use nitrogen gas
as in the case ofthe above-describedembodiment, because
the cost can be reduced.
In addition, in the above-described embodiment, the
case where the low-rank coal 1 is pyrolyzed by heating
15 is described. However, the present invention is not
limited to this case, and the present invention can be
applied to any case in the same manner as in the
above-described embodiment, as long as a solid organic
material is pyrolyzedby heating, and the same operations
20 and effects as those in the above-described embodiment
can be obtained.
Industrial Applicability
When the pyrolysis apparatus according to the
present invention is appliedto, for example, a case where
25 a low-rank coal (low-quality coal) such as lignite or
sub-bituminous coal is pyrolyzed, the entire low-rank
coal can be pyrolyzed with a desired pyrolysis ratio and
with high precision, Hence, the pyrolysis apparatus
according to the present invention can be used extremely
30 industrially advantageously.
Reference Signs List
1 low-rank coal (low-quality coal)
2 pyrolyzed coal
3 pyrolysis gas
5 4 standard gas
5 fuel
6 air
7 combustion gas
100 pyrolysis apparatus
PO 111 outer cylinder
112 inner cylinder
113 supply feeder
113a driving motor
114 supply hopper
15 115 standard gas supply source
115a flow amount adjustment valve
116 chute
117 combustion furnace
118 fuel supply source
20 118a flow amount adjustment valve
119 air blower
130 arithmetic control device
131 gas concentration measurement device

Claims :
1. A pyrolysis apparatus, characterized in that
the pyrolysis apparatus comprises:
a furnace main body in which a solid organic
material flows;
organicmaterial supply means for supplyingthe
organic material into the furnace main body;
heating means for heating the organic material
in the furnace main body;
sending-out means for sending out a solid
pyrolysis productandapyrolysis gas resulting from
the heating and pyrolysis in the furnace main body;
standard gas supply means for adding a standard
gas including an inert gas to the pyrolysis gas;
gas concentration measurement means for
measuring a concentration Cs ofthe standard gas and
a concentration Cc of an analyte gas including at
least one of carbon monoxide, carbon dioxide,
hydrogengas, hydrocarbongases, andH20inamixture
gas of the pyrolysis gas and the standard gas sent
out of the sending-out means; and
arithmetic control means for
calculating an amount Fc ofthe analyte gas
generated per unit weight of the organic
material by the following formula (1) on the
basis ofthe concentration Cc ofthe analyte gas
and the concentration Cs of the standard gas
measured by the gas concentration measurement
means, a flow amount Fs per unit time of the
standard gas added fromthe standard gas supply
means, and a weight Wo of the organic material
suppliedper unit time fromthe organicmaterial
supply means into the furnace main body,
determining a pyrolysis ratio Dt per unit
weight of the organic material from a map being
inputted in advance and showing a relationship
between the amount Fc of the analyte gas
generated and a pyrolysis ratio per unit weight
of the organic material, and
controlling the heating means to make the
pyrolysis ratio Dt equal to a desired pyrolysis
ratio Dr:
FC={ FS (CC/CS) ) /WO (1) a
15 2. The pyrolysis apparatus according to claim 1,
characterized in that
the arithmetic control means controls the
heating means to raise a heating temperature of the
organic material, when the pyrolysis ratio Dt is
lower than the pyrolysis ratio Dr.
3 . The pyrolysis apparatus according to claim 1 or 2,
characterized in that
the arithmetic control means controls the
heating means to lower a heating temperature of the
organic material, when the pyrolysis ratio Dt is
higher than the pyrolysis ratio Dr,
4. The pyrolysis apparatus according to any one of
30 claims 1 to 3, characterized in that
the heating means heats the furnace main body
from outside.
5. The pyrolysis apparatus according to any one of
5 claims 1 to 4, characterized in that
the standard gas supply means supplies the
standard gas to the furnace main body on an upstream
side thereof in a flow direction of the organic
material.
6. The pyrolysis apparatus according to any one of
claims 1 to 5, characterized in that
the organic material is a low-rank coal.