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 organic material
(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 heatedgas into an outer 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 t 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,
anditispossiblethatthe 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 furnace main body in which a solid organic material
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;
sending-out means for sending out a solid pyrolysis
product and a pyrolysis gas resulting from the heating
and pyrolysis in the furnace main body;
standard gas supply means for adding a standard gas
including nitrogen gas to the pyrolysis gas;
test gas production means for sending out a test gas
formed by completely combusting a mixture gas of the
pyrolysis gas and the standard gas sent out of the
sending-out means with air for complete combustion;
test gas flow amount measurement means for measuring
a flow amount Fi per unit time of the test gas sent out
of the test gas production means;
gas concentration measurement means for measuring
a concentration Cc of carbon dioxide and a concentration
Cn of nitrogen gas in the test gas; and
arithmetic control means for
calculating a flow amount Fn per unit time of
nitrogen gas in the mixture gas completely combusted by
the test gas production means by the following formula
(1) on the basis of the flow amount Fi measured by the
test gas flow amount measurement means and the
concentration Cn measured by the gas concentration
measurement means,
calculating a generated amount Wc per unit time of
carbon components in the pyrolysis gas sent out of the
sending-out means by the following formula (2) on the
basis of a flow amount Fs per unit time of the standard
gas supplied from the standard gas supply means to the
pyrolysis gas, a flow amount Fa per unit time of the air
for complete combustion used in the test gas production
means, the flow amount Fn calculated by the following
formula (I), the flow amount Fi measured by the test gas
flow amount measurement means, and the concentration Cc
measured by the gas concentration measurement means,
calculating a pyrolysis ratio Dt of the pyrolysis
5 product sent out ofthe sending-out means by the following
formula (3) on the basis of a weight Wo of the organic
material supplied per unit time into the furnace main
body by the organic material supply means, the generated
amount Wc calculated by the following formula (2), and
10 a concentration Cg of carbon components in the organic
material inputted in advance, and
controlling the heating means to make the pyrolysis
ratio Dt equal to a desired pyrolysis ratio Dr:
Fn=FixCn (I),
15 Wc={ (FixCc) / (Fn-0.78lxFa) }xi (Fs/22.4) xl2) (2) ,and
Dt= (Wc/Cg) /Wo ( 3 ) .
Meanwhile, a pyrolysis apparatus according to a
secondaspect ofthe invention is the pyrolysis apparatus
according to the first aspect of the invention,
20 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,
25 Meanwhile, a pyrolysis apparatus according to a
third aspect of the invention is the pyrolysis apparatus
according tothe first or second aspect ofthe invention,
characterized in that
the arithmetic control means controls the heating
30 means to lower a heating temperature of the organic
material, when the pyrolysis ratio Dt is higher than the
pyrolysis ratio Dr.
Meanwhile, a pyrolysis apparatus according to a
fourthaspect ofthe invention is the pyrolysis apparatus
5 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
outside.
Meanwhile, a pyrolysis apparatus according to a
PO 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
the standard gas supply means supplies the standard
gas to the furnace main body on an upstream side thereof
15 in a flow direction of the organic material.
Meanwhile, a pyrolysis apparatus according to a
sixth aspect of the invention is the pyrolysis apparatus
according to any one of the first to fifth aspects of
the invention, characterized in that
20 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
flow amount Fn by the above-described formula (1) on the
25 basis of the flow amount Fi and the concentration Cn,
calculates the generated amount Wc by the
above-described formula (2) on the basis of the flow
amounts Fs, Fa, Fn, and Fi and the concentration Cc,
calculates the pyrolysis ratio Dtbythe above-described
30 formula (3) on the basis of the weight Wo, the generated
amount Wc, and the concentration Cg, and controls the
heating means to make the pyrolysis ratio Dt equal to
a desired pyrolysis ratio Dr. Hence, the amount of heat
applied to the organic material can be set on the basis
5 of the pyrolysis ratio (degree) of the entire organic
material after the completion of pyrolysis. Therefore,
even when the temperature of the organic material in the
furnace main body greatly varies depending on the
position, the entire organic material can be heated with
10 a necessary and sufficient amount of heat without being
influenced by the variation. Consequently, the entire
organic material can be pyrolyzed with a desired
pyrolysis ratio Dr and with high precision.
B r i e f D e s c r i p t i o n of D r a w i n g s
Fig. 1 is a schematic structural diagram of a main
embodiment of a pyrolysis apparatus according to the
present invention.
D e s c r i p t i o n of E m b o d i m e n t s
Embodiments of a pyrolysis apparatus according to
20 the present invention are described based on the
drawings; however, the present invention is not limited
exclusivelytothe following embodiments describedbased
on the drawings.
Amain embodiment of a pyrolysis apparatus according
to the present invention is described based on Fig. 1.
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
left side in Fig. 1) of the inner cylinder 112, a tip
5 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 a driedlow-rank
coal (low-quality coal) 1 such as lignite or
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
source 115 which is standard gas supply means for
15 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
the inner cylinder 112, a chute 116 is connected to the
20 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 solidpyrolysis productobtainedbypyrolyzing
the low-rank coal 1, and for sending out pyrolysis gas
25 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
combusted.
30 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
therebetween. In addition, an air blower 119 for
supplying air 6 for combustion into the combustion
6 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
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
1lla is connected through which the combustion gas 7 fed
into the outer cylinder 111 is emitted to the outside
15 of the system.
A portion between the upper portion of the chute 116
and the combustion furnace 117 is connected to a small
combustor 120 for taking out and completely combusting
an aliquot of a mixture gas of the pyrolysis gas 3 and
20 the standard gas 4 sent out of the chute 116. To the
combustor 120, a small air blower 121 for feeding air
8 for complete combustion is connected, and the combustor
120 is configured such that a test gas 9 in which all
carbon components in the mixture gas are oxidized to
25 carbon dioxide (completely combusted) by combusting the
mixture gas taken out together with the air 8 from the
air blower 121 can be produced and sent out.
A gas outlet of the combustor 120 is connected to
a gas concentration measurement device 131, such as a
30 gas chromatograph, which is gas concentration
measurement means for measuring the concentrations of
components such as carbon dioxide and nitrogen gas in
the test gas 9 sent out through the gas outlet. A gas
flow meter 132 is provided near the gas outlet of the
combustor 120. The gas flow meter 132 is test gas flow
5 amount measurement means for measuring the flow amount
of the test gas 9 sent out through the gas outlet. A
portion between the gas flow meter 132 and the gas
concentration measurement device 131 communicates with
the outside of the system. The gas concentration
10 measurement device 131 and the gas flow meter 132 are
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
15 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 I18 ,. and
the air blowers 119 and121. The arithmetic control device
130 is configured such that the arithmetic control device
20 130 can control operations of the driving motor 113a,
the flow amount adjustment valves 115a and 118a, the air
blowers 119 and 121, and the like on the basis of
information from the gas concentration measurement
device 131 and the gas flow meter 132, information
25 inputted in advance, and the like (details 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, heating means is
30 constituted by the outer cylinder 111, the combustion
furnace 117, the fuel supply source 118, the air blower
119, and the like, and test gas production means is
constituted by the combustor 120, the air blower 121,
and the like.
Next, operations of such a pyrolysis apparatus 100
5 according to this embodiment are described.
After introduction of the low-rank coal 1 into the
supply hopper 114, the type of the low-rank coal 1, a
desired pyrolysis ratio (degree) Dr of the low-rank coal
1, a weight Wo of the low-rank coal 1 supplied per unit
10 time into the inner cylinder 112, a flow amount Fs per
unit time of the standard gas 4 supplied into the inner
cylinder 112, and a flow amount Fa per unit time of the
air 8 supplied to the combustor 120 are inputted to the
arithmetic control device 130, and the inner cylinder
15 112 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 inputted weight Wo per unit
time, and controls an operation of the flow amount
20 adjustment valve 115a of the nitrogen gas supply source
115 to supply the nitrogen gas 4 into the inner cylinder
112 at the inputted flow amount Fs per unit time.
Moreover, the arithmetic control device 130 controls an
operation of the air blower 121 to supply the air 8 to
25 the combustor 120 at the inputted flow amount Fa per unit
time. On the other hand, the arithmetic control device
130 controls operations of the flow amount adjustment
valve118a ofthe fuel supply source118 andthe airblower
119 to feed the fuel 5 and the air 6 at standard flow
30 amounts for the beginning of the operations, so that
combustion gas 7 is generated at a standard temperature
in the combustion furnace 117 and fed into the outer
cylinder 111.
With the rotation of the inner cylinder 112, the
low-rankcoallsuppliedintotheinner cylinder112moves
5 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.
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
PO fed into the outer cylinder 111, and pyrolyzed into
pyrolyzed coal 2, which is sent out to the chute 116,
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
15 inner cylinder 112 is emittedtothe outside ofthe system
through the exhaust line Illa.
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
20 112 with the standard gas 4 supplied from the standard
gas supply source 115 into the inner cylinder 112 on an
upstream side thereof in the flow direction of the
low-rank coal 1 to form a mixture gas with the standard
gas 4. The mixture gas is sent out through the upper
25 portion of the chute 116. While an aliquot of the mixture
gas is taken out to the combustor 120, the rest is fed
into the combustion furnace 117, 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.
30 The mixture gas taken out to the combustor 120 is
combusted with the air 8 to form a test gas 9 in which
all carbon components are oxidized to carbon dioxide
(completely combusted). The test gas 9 is sent out of
the combustor 120, and the flow amount of the test gas
9ismeasuredwiththegas flowmeter 132. Then, an aliquot
5 of the test gas 9 is taken out to the gas concentration
measurement device 131, whereas the rest is emitted to
the outside of the system.
The gas concentration measurement device 131
measures constituent ratios (concentrations) of carbon
PO dioxide and nitrogen gas in the test gas 9 taken out,
and transmits the information to the arithmetic control
device 130.
The arithmetic control device 130 calculates a flow
amount Fn per unit time of nitrogen gas in the mixture
15 gas supplied to the combustor 120, i. e., the mixture gas
completely combusted in the combustor 120 by the
following formula (1) on the basis of information from
the gas flow meter 132, i.e., a flow amount Fi per unit
time of the test gas 9 sent out of the combustor 120 and
20 information from the gas concentration measurement
device 131, i.e., a constituent ratio (concentration)
Cn of nitrogen gas in the test gas 9:
Fn=FixCn (1)
Moreover, the arithmetic control device 130
25 calculates a generated amount (weight) Wc per unit time
of carbon components in the pyrolysis gas 3 by the
following formula (2) on the basis of the previously
inputted flow amount Fs per unit time of the standard
gas 4 supplied into the inner cylinder 112, a flow amount
30 Fa per unit time of the air 8 supplied to the combustor
120 used in the combustor 120 for complete combustion
o f c a r b o n c o m p o n e n t s i n t h e m i x t u r e g a s , i . e . , p r e v i o u s l y
i n p u t t e d , t h e flow amount Fn, t h e flow amount F i , and
i n f o r m a t i o n from t h e g a s c o n c e n t r a t i o n measurement
d e v i c e 1 3 1 , i . e . , t h e c o n s t i t u e n t r a t i o ( c o n c e n t r a t i o n )
5 C c of c a r b o n d i o x i d e i n t h e t e s t g a s 9 :
Wc={ ( F i x C c ) / (Fn-0,781xF'a) } x { ( F s / 2 2 * 4 ) ~ 1 2(2 ).
Then, t h e a r i t h m e t i c c o n t r o l d e v i c e 130 c a l c u l a t e s
t h e p y r o l y s i s r a t i o ( d e g r e e ) D t of t h e p y r o l y z e d c o a l
2 s e n t o u t t h r o u g h t h e c h u t e 116 by t h e f o l l o w i n g f o r m u l a
10 ( 3 ) on t h e b a s i s of t h e p r e v i o u s l y i n p u t t e d w e i g h t Wo
of t h e low-rank c o a l 1 s u p p l i e d p e r u n i t t i m e i n t o t h e
i n n e r c y l i n d e r 112, t h e g e n e r a t e d amount ( w e i g h t ) W c ,
and t h e c o n s t i t u e n t r a t i o ( c o n c e n t r a t i o n ) Cg o f c a r b o n
components i n t h e low-rank c o a l 1 f o r t h e p r e v i o u s l y
15 i n p u t t e d t y p e o f t h e low-rank c o a l 1 i n p u t t e d i n a d v a n c e :
Dt= (Wc/Cg) /Wo ( 3 ) .
Then, t h e a r i t h m e t i c c o n t r o l d e v i c e 130 c o m p a r e s t h e
p y r o l y s i s r a t i o ( d e g r e e ) D t of t h e p y r o l y z e d c o a l 2 w i t h
t h e p r e v i o u s l y i n p u t t e d d e s i r e d p y r o l y s i s r a t i o ( d e g r e e )
20 D r . When t h e p y r o l y s i s r a t i o ( d e g r e e ) D t t a k e s a v a l u e
w i t h i n t h e r a n g e o f a n a l l o w a b l e e r r o r of t h e p y r o l y s i s
r a t i o ( d e g r e e ) D r , t h e a r i t h m e t i c c o n t r o l d e v i c e 130
d e t e r m i n e s t h a t t h e low-rank c o a l 1 i s p y r o l y z e d w i t h
t h e d e s i r e d p y r o l y s i s r a t i o ( d e g r e e ) D r and c o n t r o l s an
25 o p e r a t i o n of t h e f l o w amount a d j u s t m e n t v a l v e 118a of
t h e f u e l s u p p l y s o u r c e 118 t o f e e d t h e f u e l 5 a t t h e
c u r r e n t f l o w amount.
On t h e o t h e r hand, when t h e p y r o l y s i s r a t i o ( d e g r e e )
D t t a k e s a v a l u e which i s n o t w i t h i n t h e r a n g e of t h e
30 a l l o w a b l e e r r o r of t h e p y r o l y s i s r a t i o ( d e g r e e ) D r , and
which i s s m a l l e r t h a n t h e p y r o l y s i s r a t i o ( d e g r e e ) D r
(DtDr), the arithmetic control device 130 determines
that the loss (in weight) on pyrolysis per unit weight
15 ofthe low-rank coal1 is 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
20 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.
25 Specifically, the concentration Cc of carbon dioxide in
the test gas 9 obtained by taking out and completely
combusting an aliquot of the pyrolysis gas 3 after the
completion of pyrolysis sent out through the chute 116
together with the pyrolyzed coal 2 after the pyrolysis
30 is detected, and the generated amount Wc of carbon
components in the pyrolysis gas 3 is calculated from the
concentration Cc of carbon dioxide. Thus, the pyrolysis
ratio (degree) Dt of the pyrolyzed coal 2 is determined
on the basis of the constituent ratio (concentration)
Cg of carbon components in the low-rank coal 1 for the
5 type of the low-rank coal 1 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
to the low-rank coal 1 can be set on the basis of the
10 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
15 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
20 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.
25 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
30 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
5 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, sothat it tend sto be difficult to accurately
measure the flow amount of the pyrolysis gas 3.
In addition, even if an extremely small amount of
oxygen gas, hydrogen gas, or the like enter the inner
cylinder 112 from the outside, and the low-rank coal 1
in an amount corresponding tothe amount ofthe gas should
be combusted and lost, the entire low-rank coal 1 can
15 be pyrolyzed with a desiredpyrolysis ratio Dr, and hence
the yield of the pyrolyzed coal 2 can be stabilized.
In addition, even when H20 or the like enters the
inner cylinder 112 from the outside, the H20 or the like
does not exert any influence on the calculation of the
20 generatedamountwc of carbon components in the pyrolysis
gas 3. Hence, the pyrolysis ratio (degree) Dt of the
pyrolyzed coal 2 can be determined stably, without being
influenced by the amount of water in the inner cylinder
112.
25 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
side in the flow directionofthelow-rankcoallto supply
the standard gas 4 into the inner cylinder 112.
30 Alternatively, as another embodiment, it is also
possibleto, for example, connect the standardgas supply
source 115 to a position between the chute 11 6 and the
gas concentration measurement device 131 and supply the
standard gas 4 to the pyrolysis gas 3.
In addition, in the above-described embodiment, the
5 case of the pyrolysis apparatus 100 of a rotary kiln type
in which the inner cylinder 112 is rotatably supported
in the fixedly supportedouter cylinder 111 is described.
Alternatively, as another embodiment, it is also
possible, for example, to use a pyrolysis apparatus of
PO 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
15 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
possible, for example, to pyrolyze the low-rank coal 1
in the inner cylinder 112 by heating the inner cylinder
20 112 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
cylinder 112 with the combustion gas 7 as in the case
ofthe above-describedembodiment, because the pyrolysis
25 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.
In addition, in the above-described embodiment, the
combustion gas 7 is fed into the outer cylinder 111, and
30 the pyrolysis is conducted by heating the low-rank coal
1 indirectly through the inner cylinder 112.
Alternatively, as another embodiment, it is also
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
5 exchanger, supply theheated standardgas 4 into the inner
cylinder 112, and conduct the pyrolysis by directly
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
10 the inner cylinder 112, and conduct the pyrolysis by
directly heating the low-rank coal 1, because a large
amount of the standard gas 4 has to be used, and the cost
increases.
In addition, in the above-described embodiment, the
15 case where the low-rank coal 1 is pyrolyzed by heating
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
20 material is pyrolyzedbyheating, and the same operations
and effects as those in the above-described embodiment
can be obtained.
Industrial Applicability
When the pyrolysis apparatus according to the
25 present invention is appliedto, for example, a casewhere
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
industrially advantageously.
Reference Signs List
1 low-rank coal (low-quality coal)
5 2 pyrolyzed coal
3 pyrolysis gas
4 standard gas
5 fuel
6 air
10 7 combustion gas
8 air
9 test gas
100 pyrolysis apparatus
111 outer cylinder
15 112 inner cylinder
113 supply feeder
113a driving motor
114 supply hopper
115 standard gas supply source
20 115a flow amount adjustment valve
116 chute
117 combustion furnace
118 fuel supply source
118a flow amount adjustment valve
25 119 air blower
120 combustor
121 air blower
130 arithmetic control device
131 gas concentration measurement device
30 132 gas flow meter

Claims :
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 productanda pyrolysis gas resulting from
the heating and pyrolysis in the furnace main body;
standard gas supply means for adding a
standardgas including nitrogen gas tothe pyrolysis
gas;
test gas productionmeans for sending out atest
gas formed by completely combusting a mixture gas
of the pyrolysis gas and the standard gas sent out
of the sending-out means with air for complete
combustion;
test gas flow amount measurement means for
measuring a flow amount Fi per unit time of the test
gas sent out of the test gas production means;
gas concentration measurement means for
measuring a concentration Cc of carbon dioxide and
a concentration Cn of nitrogen gas in the test gas;
and
arithmetic control means for
calculating a flow amount Fn per unit time
of nitrogen gas in the mixture gas completely
combusted by the test gas production means by
the following formula (1) on the basis of the
flow amount Fi measured by the test gas flow
amount measurement means and the concentration
Cn measured by the gas concentration
measurement means,
calculating a generated amount Wc per unit
time of carbon components in the pyrolysis gas
sent out of the sending-out means by the
following formula (2) on the basis of a flow
amount Fs per unit time of the standard gas
supplied from the standard gas supply means to
the pyrolysis gas, a flow amount Fa per unit time
of the air for complete combustion used in the
test gas production means, the flow amount Fn
calculated by the following formula (I), the
flow amount Fi measured by the test gas flow
amountmeasurementmeans, andthe concentration
Cc measured by the gas concentration
measurement means,
calculating a pyrolysis ratio Dt of the
pyrolysis product sent out of the sending-out
means by the following formula (3) on the basis
of a weight Wo of the organic material supplied
per unit time into the furnace main body by the
organic material supply means, the generated
amount Wc calculated by the following formula
(2), anda concentrationcgof carboncomponents
in the organicmaterialinputtedinadvance, and
controlling the heating means to make the
pyrolysis ratio Dt equal to a desired pyrolysis
ratio Dr:
Fn=Fi xCn (I),
Wc={ (FixCc) / (Fn-0.78lxFa) }x{ (Fs/22.4)~12} (2),
and
Dt= (Wc/Cg) /Wo ( 3 ) .
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.
15
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
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
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
5 claims 1 to 5, characterized in that
the organic material is a low-rank coal.