U.S. patent application number 13/813583 was filed with the patent office on 2013-05-23 for method and apparatus of hydrolytic saccharification of cellulosic biomass.
This patent application is currently assigned to KAWASAKI JUKOGYO KABUSHIKI KAISHA. The applicant listed for this patent is Noriaki Izumi, Hiromasa Kusuda, Takeshi Nishino, Hironori Tajiri, Kunihiko Tanaka, Shoji Tsujita. Invention is credited to Noriaki Izumi, Hiromasa Kusuda, Takeshi Nishino, Hironori Tajiri, Kunihiko Tanaka, Shoji Tsujita.
Application Number | 20130125877 13/813583 |
Document ID | / |
Family ID | 45892332 |
Filed Date | 2013-05-23 |
United States Patent
Application |
20130125877 |
Kind Code |
A1 |
Kusuda; Hiromasa ; et
al. |
May 23, 2013 |
METHOD AND APPARATUS OF HYDROLYTIC SACCHARIFICATION OF CELLULOSIC
BIOMASS
Abstract
The hydrolytic saccharification method and hydrolytic
saccharification apparatus according to the present invention use a
hydraulic cylinder-type pressurized reactor as a reactor for
causing cellulosic biomass to be in a supercritical or subcritical
state, and use a hydraulic cylinder-type steam compressor as a
source of superheated steam, such that the reactor and the
compressor are operated in conjunction with each other. Surplus
hydraulic pressure that is generated when hydrolysis of the
cellulosic biomass is completed is recovered as compression power
of the hydraulic cylinder-type steam compressor. Moreover, flash
steam generated from slurry containing a hydrolysate is supplied to
the hydraulic cylinder-type steam compressor for cyclic use of the
flash steam.
Inventors: |
Kusuda; Hiromasa; (Kobe-shi,
JP) ; Izumi; Noriaki; (Kobe-shi, JP) ; Tajiri;
Hironori; (Kobe-shi, JP) ; Tsujita; Shoji;
(Itami-shi, JP) ; Nishino; Takeshi; (Suita-shi,
JP) ; Tanaka; Kunihiko; (Kobe-shi, JP) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Kusuda; Hiromasa
Izumi; Noriaki
Tajiri; Hironori
Tsujita; Shoji
Nishino; Takeshi
Tanaka; Kunihiko |
Kobe-shi
Kobe-shi
Kobe-shi
Itami-shi
Suita-shi
Kobe-shi |
|
JP
JP
JP
JP
JP
JP |
|
|
Assignee: |
KAWASAKI JUKOGYO KABUSHIKI
KAISHA
Kobe-shi, Hyogo
JP
|
Family ID: |
45892332 |
Appl. No.: |
13/813583 |
Filed: |
September 27, 2011 |
PCT Filed: |
September 27, 2011 |
PCT NO: |
PCT/JP2011/005420 |
371 Date: |
January 31, 2013 |
Current U.S.
Class: |
127/1 ;
127/37 |
Current CPC
Class: |
D21C 5/00 20130101; C13K
1/02 20130101; C10L 1/02 20130101 |
Class at
Publication: |
127/1 ;
127/37 |
International
Class: |
D21C 5/00 20060101
D21C005/00 |
Foreign Application Data
Date |
Code |
Application Number |
Sep 30, 2010 |
JP |
2010-221707 |
Claims
1. A method of hydrolytic saccharification of cellulosic biomass,
in which cellulosic biomass is hydrolytically saccharified by
pressurizing slurry of the cellulosic biomass together with
superheated steam into a supercritical or subcritical state in at
least one hydraulic cylinder-type pressurized reactor, the method
comprising: supplying, by at least one hydraulic cylinder-type
steam compressor, the superheated steam to the hydraulic
cylinder-type pressurized reactor; recovering hydraulic pressure of
a hydraulic pressure chamber of the hydraulic cylinder-type
pressurized reactor into a hydraulic pressure chamber of the
hydraulic cylinder-type steam compressor at a time of reducing
pressure in the hydraulic cylinder-type pressurized reactor to a
pressure of the supercritical or subcritical state or lower after
the cellulosic biomass has been hydrolytically saccharified,
wherein a hydraulic pressure return passage of the hydraulic
cylinder-type pressurized reactor and the hydraulic pressure
chamber of the hydraulic cylinder-type steam compressor are in a
state of connection via a hydraulic pressure recovery passage; and
after supplying the slurry, the cellulosic biomass of which has
been hydrolytically saccharified, into a flash tank,
flash-evaporating the slurry and recovering flash steam into the
hydraulic cylinder-type steam compressor.
2. The method of hydrolytic saccharification of cellulosic biomass
according to claim 1, wherein the at least one hydraulic
cylinder-type pressurized reactor comprises a plurality of
hydraulic cylinder-type pressurized reactors, and the at least one
hydraulic cylinder-type steam compressor comprises a plurality of
hydraulic cylinder-type steam compressors, and the number of
hydraulic cylinder-type steam compressors, which perform the
supplying of the superheated steam to the hydraulic cylinder-type
pressurized reactors, is the same as the number of hydraulic
cylinder-type pressurized reactors, the method comprising
cyclically recovering the hydraulic pressure of the hydraulic
pressure chamber of each hydraulic cylinder-type pressurized
reactor into the hydraulic pressure chamber of a corresponding one
of the hydraulic cylinder-type steam compressors at the time of
reducing the pressure in the hydraulic cylinder-type pressurized
reactor to the pressure of the supercritical or subcritical state
or lower after the cellulosic biomass has been hydrolytically
saccharified, wherein the hydraulic pressure return passage of each
hydraulic cylinder-type pressurized reactor and the hydraulic
pressure chamber of the corresponding hydraulic cylinder-type steam
compressor are in the state of connection via the hydraulic
pressure recovery passage.
3. The method of hydrolytic saccharification of cellulosic biomass
according to claim 1, wherein the hydraulic pressure recovery
passage is formed as a single passage at a portion connecting to
the hydraulic pressure return passage and at a portion connecting
to the hydraulic pressure chamber of the hydraulic cylinder-type
steam compressor, and a remaining portion of the hydraulic pressure
recovery passage is divided into a plurality of sub-passages, and
each sub-passage is provided with a corresponding one of air
chambers which are assigned different pressure storage setting
values, respectively, the method comprising: storing the hydraulic
pressure of the hydraulic pressure chamber of the hydraulic
cylinder-type pressurized reactor sequentially in the air chambers
in descending order of the pressure storage setting value; and then
releasing the hydraulic pressure sequentially from the air chambers
in ascending order of the pressure storage setting value to supply
the hydraulic pressure to the hydraulic pressure chamber of the
hydraulic cylinder-type steam compressor.
4. The method of hydrolytic saccharification of cellulosic biomass
according to claim 1, wherein a steam generator is connected to the
flash tank, the method comprising: mixing steam supplied from the
steam generator and the flash steam; and supplying resultant steam
to the hydraulic cylinder-type steam compressor.
5. The method of hydrolytic saccharification of cellulosic biomass
according to claim 1, wherein an air and/or nitrogen supply device
is connected to at least one of the flash tank and steam piping
connecting the flash tank and the hydraulic cylinder-type steam
compressor, the method comprising mixing air and/or nitrogen into
steam to be supplied to a steam compression chamber of the
hydraulic cylinder-type steam compressor, such that the air and/or
nitrogen mixed into the steam is in an amount that is not less than
1/7 and not more than 1/3 of an amount of the steam.
6. An apparatus for hydrolytic saccharification of cellulosic
biomass comprising: at least one hydraulic cylinder-type
pressurized reactor configured to pressurize slurry of cellulosic
biomass together with superheated steam into a supercritical or
subcritical state; at least one hydraulic cylinder-type steam
compressor configured to supply the superheated steam to the
hydraulic cylinder-type pressurized reactor; and a flash tank
configured to be supplied with the slurry that is removed from the
hydraulic cylinder-type pressurized reactor, the slurry being in a
high-temperature and high-pressure state, and to flash-evaporate
the slurry, wherein a hydraulic pressure return passage of the
hydraulic cylinder-type pressurized reactor and a hydraulic
pressure chamber of the hydraulic cylinder-type steam compressor
are connected via a hydraulic pressure recovery passage, hydraulic
pressure of a hydraulic pressure chamber of the hydraulic
cylinder-type pressurized reactor is recovered into the hydraulic
pressure chamber of the hydraulic cylinder-type steam compressor
through the hydraulic pressure recovery passage, the flash tank is
connected to the hydraulic cylinder-type steam compressor, and
flash steam generated from the slurry in the high-temperature and
high-pressure state is recovered into the hydraulic cylinder-type
steam compressor.
7. The apparatus for hydrolytic saccharification of cellulosic
biomass according to claim 6, wherein the at least one hydraulic
cylinder-type pressurized reactor comprises a plurality of
hydraulic cylinder-type pressurized reactors, and the at least one
hydraulic cylinder-type steam compressor comprises a plurality of
hydraulic cylinder-type steam compressors, the number of hydraulic
cylinder-type steam compressors, which supply the superheated steam
to the hydraulic cylinder-type pressurized reactors, is the same as
the number of hydraulic cylinder-type pressurized reactors, the
hydraulic pressure return passage of each hydraulic cylinder-type
pressurized reactor is connected to the hydraulic pressure chamber
of a corresponding one of the hydraulic cylinder-type steam
compressors via the hydraulic pressure recovery passage, the
hydraulic pressure of the hydraulic pressure chamber of each
hydraulic cylinder-type pressurized reactor is recovered into the
hydraulic pressure chamber of the corresponding hydraulic
cylinder-type steam compressor via the hydraulic pressure recovery
passage, the flash tank is connected to the plurality of hydraulic
cylinder-type steam compressors, and the flash steam generated from
the slurry in the high-temperature and high-pressure state is
cyclically recovered into the plurality of hydraulic cylinder-type
steam compressors.
8. The apparatus for hydrolytic saccharification of cellulosic
biomass according to claim 6, wherein the hydraulic pressure
recovery passage is formed as a single passage at a portion
connecting to the hydraulic pressure return passage and at a
portion connecting to the hydraulic pressure chamber of the
hydraulic cylinder-type steam compressor, and a remaining portion
of the hydraulic pressure recovery passage is divided into a
plurality of sub-passages, each sub-passage is provided with a
corresponding one of air chambers which are assigned different
pressure storage setting values, respectively, and the hydraulic
pressure of the hydraulic pressure chamber of the hydraulic
cylinder-type pressurized reactor is sequentially stored in the air
chambers in descending order of the pressure storage setting value,
and then the hydraulic pressure is released sequentially from the
air chambers in ascending order of the pressure storage setting
value and supplied to the hydraulic pressure chamber of the
hydraulic cylinder-type steam compressor.
9. The apparatus for hydrolytic saccharification of cellulosic
biomass according to claim 6, wherein a steam generator is
connected to the flash tank, and steam supplied from the steam
generator and the flash steam are mixed, and then resultant steam
is supplied to the hydraulic cylinder-type steam compressor.
10. The apparatus for hydrolytic saccharification of cellulosic
biomass according to claim 6, wherein an air and/or nitrogen supply
device is connected to at least one of the flash tank and steam
piping connecting the flash tank and the hydraulic cylinder-type
steam compressor, and air and/or nitrogen is mixed into steam to be
supplied to a steam compression chamber of the hydraulic
cylinder-type steam compressor, such that the air and/or nitrogen
mixed into the steam is in an amount that is not less than 1/7 and
not more than 1/3 of an amount of the steam.
Description
TECHNICAL FIELD
[0001] The present invention relates to a method and apparatus for
use in producing saccharides by hydrolyzing cellulosic biomass in a
supercritical or subcritical state.
BACKGROUND ART
[0002] As part of biomass energy utilization, attempts have been
made to obtain ethanol (bioethanol) by hydrolyzing cellulose or
hemicellulose, which are major components of plants. Ethanol thus
obtained is planned to be utilized mainly as a fuel to be mixed
into an automobile fuel or as an alternative fuel for gasoline.
[0003] Major components of plants include cellulose (a polymer of
glucose which is a C6 monosaccharide composed of six carbon atoms),
hemicellulose (a polymer of C5 and C6 monosaccharides; a C5
monosaccharide is composed of five carbon atoms), lignin, and
starch. Ethanol is produced by using saccharides as raw materials,
such as a C5 monosaccharide, a C6 monosaccharide, and an
oligosaccharide which is a complex of these saccharides. Ethanol is
produced through fermentation of microorganisms such as yeast.
[0004] For hydrolyzing cellulosic biomass containing cellulose or
hemicellulose into saccharides, there are the following three
possible methods to be industrially applied: 1) a method of
hydrolyzing such biomass by utilizing oxidizing power of a strong
acid such as sulfuric acid; 2) a method of hydrolyzing such biomass
by utilizing an enzyme; and 3) a method utilizing oxidizing power
of supercritical or subcritical water. However, the acidolysis
method 1) indispensably requires a treatment for neutralizing the
added acid after hydrolysis of cellulose or hemicellulose into
saccharides and before fermentation of the saccharides into ethanol
because the added acid acts as an inhibitor against the
fermentation by yeast. The cost of such treatment makes it
difficult to put this method into practical use from an economic
standpoint. Although the enzymolysis method 2) can be realized by a
process under a normal temperature and constant pressure, no
effective enzyme for the method has been found yet, and even if an
effective enzyme is found, the outlook for industrial-scale
realization of the method is still unclear in terms of cost
efficiency, because such an enzyme is expected to incur a high
production cost thereof.
[0005] As the method 3) of hydrolyzing cellulosic biomass into
saccharides by using supercritical or subcritical water, there are
disclosed methods as described below. Patent Literature 1 discloses
a method of producing water-insoluble polysaccharides, which is
characterized by hydrolysis of cellulose powder that is performed
by bringing the powder into contact with pressurized hot water of
240 to 340.degree. C. Patent Literature 2 discloses a method
including: hydrolyzing biomass chips for a predetermined time
period with hot water pressurized to a saturated vapor pressure or
higher at 140 to 230.degree. C., thereby extracting hemicellulose;
and then hydrolyzing the biomass chips with pressurized hot water
heated to a temperature not lower than a cellulose hydrolyzing
temperature, thereby extracting cellulose. Patent Literature 3
discloses a method of producing glucose and/or water-soluble
cello-oligosaccharides, which is characterized in that cellulose
having a mean polymerization degree of not less than 100 is
hydrolyzed by: bringing the cellulose into contact reaction with
supercritical or subcritical water at a temperature of not lower
than 250.degree. C. and not higher than 450.degree. C. and at a
pressure of not lower than 15 MPa and not higher than 450 MPa for a
time period of not less than 0.01 second and not more than 5
seconds; then cooling down the cellulose; and thereafter bringing
the cellulose into contact with subcritical water at a temperature
of not lower than 250.degree. C. and not higher than 350.degree. C.
and at a pressure of not lower than 15 MPa and not higher than 450
MPa for a time period of not less than 1 second and not more than
10 minutes.
[0006] In the case of performing hydrolysis or oxidative
decomposition of organic matter such as biomass by using
supercritical or subcritical water, high-pressure water in which
the organic matter is dispersed is heated up quickly and a
supercritical or subcritical state is maintained for a certain
period of time, and thereby a hydrolysis reaction is caused. After
the reaction is completed, it is necessary to quickly cool down the
reaction system to stop further chemical reactions from occurring.
As one example of a reaction apparatus capable of such quick
heating and quick cooling, Patent Literature 4 discloses a reactor
which is configured to pressurize steam from a boiler by using a
piston, thereby producing supercritical or subcritical water.
Patent Literature 4 also discloses: driving the cylinder of the
reactor by means of a crank mechanism or cam mechanism; recovering
steam from a product removed from the reactor; and utilizing the
pressure of the steam for driving the crank mechanism or cam
mechanism.
[0007] Patent Literature 5 discloses an organic matter system for
supplying an organic matter-containing fluid at a stable flow rate
while keeping the fluid in a high-temperature and high-pressure
state. The system disclosed in Patent Literature 5 includes: a
first driver configured to receive a processed high-pressure fluid
and its pressure by the piston of a cylinder and transmit the
pressure as force to pressurize an unprocessed fluid; and a second
driver configured to supplement the first driver with driving
force. The system is configured to reduce the energy of the
processed high-pressure fluid by using a back pressure valve, and
then introduce the fluid into the cylinder of the first driver.
CITATION LIST
Patent Literature
[0008] PTL 1: Japanese Laid-Open Patent Application Publication No.
2000-186102
[0009] PTL 2: Japanese Laid-Open Patent Application Publication No.
2002-59118
[0010] PTL 3: Japanese Laid-Open Patent Application Publication No.
2003-212888
[0011] PTL 4: Japanese Laid-Open Patent Application Publication No.
2002-263465
[0012] PTL 5: Japanese Laid-Open Patent Application Publication No.
2000-233127
SUMMARY OF INVENTION
Technical Problem
[0013] In the apparatus disclosed in Patent Literature 4 in which
the crank mechanism or cam mechanism is driven by the recovered
steam, it is unavoidable to synchronize the timing of recovering
the steam with the timing of compressing the reactor with the
cylinder. With the apparatus disclosed in Patent Literature 4,
effective utilization of the latent heat of the steam cannot be
realized. Further, in a case where the rotational frequency of the
crank mechanism or cam mechanism is set to be constant, it is
difficult to maintain the cylinder of the reactor in a pushed state
for a certain period of time, and difficult to arbitrarily change
the speed of pushing or pulling the cylinder while in operation.
Thus, there is not much freedom in changing operating
conditions.
[0014] Also in the system disclosed in Patent Literature 5, it is
unavoidable to synchronize the driving of a primary cylinder with
the driving of a secondary cylinder since the piston of the primary
cylinder and the piston of the secondary cylinder are connected by
a single piston rod.
[0015] An object of the present invention is, in a method and
apparatus of hydrolyzing cellulosic biomass in a supercritical or
subcritical state, to reduce compression power by recovering
surplus pressure at the time of reducing the pressure in a reactor,
and to obtain freedom in the timing of operating the reactor and
the timing of operating a compression mechanism. Another object of
the present invention is to recover latent heat through cyclic use
of flash steam, thereby improving thermal efficiency.
Solution to Problem
[0016] The inventors of the present invention conducted diligent
studies to solve the above problems. As a result of the diligent
studies, the inventors arrived at using a hydraulic cylinder-type
pressurized reactor as a reactor for causing cellulosic biomass to
be in a supercritical or subcritical state, and using a hydraulic
cylinder-type steam compressor as a source of superheated steam,
and then attempted to operate the reactor and steam compressor in
conjunction with each other. Then, the inventors have found that
the above-described problems can be solved by performing the
following: recover surplus hydraulic pressure when hydrolysis of
the cellulosic biomass is completed to use the recovered pressure
as compression power of the hydraulic cylinder-type steam
compressor; and supply flash steam generated from slurry containing
a hydrolysate to the hydraulic cylinder-type steam compressor for
cyclic use of the flash steam. As a result, the inventors have
accomplished the present invention.
[0017] Specifically, the present invention relates to a method of
hydrolytic saccharification of cellulosic biomass, in which
cellulosic biomass is hydrolytically saccharified by pressurizing
slurry of the cellulosic biomass together with superheated steam
into a supercritical or subcritical state in at least one hydraulic
cylinder-type pressurized reactor. The method includes: supplying,
by at least one hydraulic cylinder-type steam compressor, the
superheated steam to the hydraulic cylinder-type pressurized
reactor; recovering hydraulic pressure of a hydraulic pressure
chamber of the hydraulic cylinder-type pressurized reactor into a
hydraulic pressure chamber of the hydraulic cylinder-type steam
compressor at a time of reducing pressure in the hydraulic
cylinder-type pressurized reactor to a pressure of the
supercritical or subcritical state or lower after the cellulosic
biomass has been hydrolytically saccharified, wherein a hydraulic
pressure return passage of the hydraulic cylinder-type pressurized
reactor and the hydraulic pressure chamber of the hydraulic
cylinder-type steam compressor are in a state of connection via a
hydraulic pressure recovery passage; and after supplying the
slurry, the cellulosic biomass of which has been hydrolytically
saccharified, into a flash tank, flash-evaporating the slurry and
recovering flash steam into the hydraulic cylinder-type steam
compressor.
[0018] The present invention also relates to an apparatus for
hydrolytic saccharification of cellulosic biomass including: at
least one hydraulic cylinder-type pressurized reactor configured to
pressurize slurry of cellulosic biomass together with superheated
steam into a supercritical or subcritical state; at least one
hydraulic cylinder-type steam compressor configured to supply the
superheated steam to the hydraulic cylinder-type pressurized
reactor; and a flash tank configured to be supplied with the slurry
that is removed from the hydraulic cylinder-type pressurized
reactor, the slurry being in a high-temperature and high-pressure
state, and to flash-evaporate the slurry. A hydraulic pressure
return passage of the hydraulic cylinder-type pressurized reactor
and a hydraulic pressure chamber of the hydraulic cylinder-type
steam compressor are connected via a hydraulic pressure recovery
passage. Hydraulic pressure of a hydraulic pressure chamber of the
hydraulic cylinder-type pressurized reactor is recovered into the
hydraulic pressure chamber of the hydraulic cylinder-type steam
compressor through the hydraulic pressure recovery passage. The
flash tank is connected to the hydraulic cylinder-type steam
compressor. Flash steam generated from the slurry in the
high-temperature and high-pressure state is recovered into the
hydraulic cylinder-type steam compressor.
[0019] Preferably, the at least one hydraulic cylinder-type
pressurized reactor comprises a plurality of hydraulic
cylinder-type pressurized reactors, and the at least one hydraulic
cylinder-type steam compressor comprises a plurality of hydraulic
cylinder-type steam compressors. Preferably, the number of
hydraulic cylinder-type steam compressors, which perform the
supplying of the superheated steam to the hydraulic cylinder-type
pressurized reactors, is the same as the number of hydraulic
cylinder-type pressurized reactors. Preferably, the method includes
cyclically recovering the hydraulic pressure of the hydraulic
pressure chamber of each hydraulic cylinder-type pressurized
reactor into the hydraulic pressure chamber of a corresponding one
of the hydraulic cylinder-type steam compressors at the time of
reducing the pressure in the hydraulic cylinder-type pressurized
reactor to the pressure of the supercritical or subcritical state
or lower after the cellulosic biomass has been hydrolytically
saccharified, wherein the hydraulic pressure return passage of each
hydraulic cylinder-type pressurized reactor and the hydraulic
pressure chamber of the corresponding hydraulic cylinder-type steam
compressor are in the state of connection via the hydraulic
pressure recovery passage.
[0020] Preferably, the hydraulic pressure recovery passage is
formed as a single passage at a portion connecting to the hydraulic
pressure return passage and at a portion connecting to the
hydraulic pressure chamber of the hydraulic cylinder-type steam
compressor, and a remaining portion of the hydraulic pressure
recovery passage is divided into a plurality of sub-passages.
Preferably, each sub-passage is provided with a corresponding one
of air chambers which are assigned different pressure storage
setting values, respectively. Preferably, the method includes:
storing the hydraulic pressure of the hydraulic pressure chamber of
the hydraulic cylinder-type pressurized reactor sequentially in the
air chambers in descending order of the pressure storage setting
value; and then releasing the hydraulic pressure sequentially from
the air chambers in ascending order of the pressure storage setting
value to supply the hydraulic pressure to the hydraulic pressure
chamber of the hydraulic cylinder-type steam compressor.
[0021] Preferably, a steam generator is connected to the flash
tank, and the method includes: mixing steam supplied from the steam
generator and the flash steam; and supplying resultant steam to the
hydraulic cylinder-type steam compressor.
[0022] Preferably, an air and/or nitrogen supply device is
connected to at least one of the flash tank and steam piping
connecting the flash tank and the hydraulic cylinder-type steam
compressor. Preferably, the method includes mixing air and/or
nitrogen into steam to be supplied to a steam compression chamber
of the hydraulic cylinder-type steam compressor, such that the air
and/or nitrogen mixed into the steam is in an amount that is not
less than 1/7 and not more than 1/3 of an amount of the steam.
[0023] The above object, other objects, features, and advantages of
the present invention will be made clear by the following detailed
description of preferred embodiments with reference to the
accompanying drawings.
ADVANTAGEOUS EFFECTS OF INVENTION
[0024] According to the present invention, compression power can be
reduced by recovering surplus pressure (surplus hydraulic pressure)
of a reactor into a steam compressor through a hydraulic passage.
Since the present invention makes it possible to recover the latent
heat of flash steam, high thermal efficiency is realized. Moreover,
according to the present invention, the reactor and the steam
compressor can be readily operated in conjunction with each other.
Furthermore, condensation of steam within the steam compressor can
be prevented by mixing air and/or nitrogen into the flash
steam.
BRIEF DESCRIPTION OF DRAWINGS
[0025] FIG. 1 is a schematic configuration diagram illustrating an
example of a processing apparatus for performing a method of
hydrolytic saccharification of cellulosic biomass according to the
present invention.
[0026] FIGS. 2A to 2D show conceptual diagrams illustrating the
operations of a hydraulic cylinder-type steam compressor 5a and a
hydraulic cylinder-type pressurized reactor 1a.
[0027] FIG. 3 is a schematic configuration diagram showing the
vicinity of the hydraulic cylinder-type steam compressor 5a and the
hydraulic cylinder-type pressurized reactor 1a of another example
of the processing apparatus for performing the method of hydrolytic
saccharification of cellulosic biomass according to the present
invention.
[0028] FIG. 4 is a schematic configuration diagram showing an
example of a conventional processing apparatus for performing a
method of hydrolytic saccharification of cellulosic biomass.
DESCRIPTION OF EMBODIMENTS
[0029] Hereinafter, embodiments of the present invention are
described with reference to the drawings.
Embodiment 1
[0030] FIG. 1 is a schematic configuration diagram showing an
example of a processing apparatus for performing a method of
hydrolytic saccharification of cellulosic biomass according to the
present invention. In FIG. 1, four hydraulic cylinder-type
pressurized reactors and four hydraulic cylinder-type steam
compressors are installed. However, the number of installed
reactors and the number of installed steam compressors are not
limited to four.
[0031] Slurry of cellulosic biomass is preheated as necessary, and
then supplied to high-pressure steam supply passages 10a to 10d
through slurry supply passages 11 and 11a to 11d. For example, the
cellulosic biomass slurry may be obtained in the following manner:
(1) vegetation biomass such as bagasse, sugar beet residue, or
straw is ground to a grain size of several millimeters or less and
then mixed with water to obtain slurry, the solid concentration of
which is approximately 20 to 50 wt %; or (2) hemicellulose in
cellulosic biomass is hydrolytically saccharified and then the
residue is dehydrated, and thereafter, the residue (i.e.,
dehydrated cake) is mixed with water to obtain slurry, the solid
concentration of which is approximately 20 to 50 wt %.
[0032] Meanwhile, steam supplied from a steam generator (not shown)
such as a boiler is supplied to a flash tank 13 through a passage
12. The steam is also supplied to steam compression chambers 8a to
8d of hydraulic cylinder-type steam compressors 5a to 5d through
recovered steam supply passages 14 and 14a to 14d. The temperature
and pressure of the steam supplied from the steam generator are
preferably in the ranges of 150 to 200.degree. C. and 0.5 to 1.6
MPa, respectively.
[0033] If the temperatures in the recovered steam supply passages
14 and 14a to 14d and the steam compression chambers 8a to 8d are
low, for example, at the start of the operation of the processing
apparatus, then the temperature of the steam supplied from the
recovered steam supply passage 14 tends to decrease. In such a
case, there is a risk that the steam is condensed within the steam
compression chambers 8a to 8d, resulting in that the latent heat of
the steam is lost. It is considered that heat-insulating the steam
piping is effective for preventing the condensation of steam during
continuous operation of the processing apparatus. However, such
heat insulation treatment results in a difficulty in heating up the
steam piping at the start of the operation.
[0034] In this respect, the processing apparatus shown in FIG. 1
optionally includes piping 28, 28a, and 28b. The piping 28 is
connected to an air and/or nitrogen supply device (not shown).
Examples of the supply devices include an air compressor, a gas
canister, and a nitrogen generator. As shown in FIG. 1, the piping
28 is divided into piping 28a and piping 28b. The piping 28a is
connected to the flash tank 13, and the piping 28b is connected to
the steam supply passages. Either the piping 28a or the piping 28b
may be eliminated.
[0035] When air and/or nitrogen are supplied from the piping 28a
and the piping 28b, the air and/or nitrogen are mixed into the
steam in the flash tank 13 and the recovered steam supply passage
14. In this manner, air and/or nitrogen can be mixed into the steam
to be supplied to the steam compression chambers 8a to 8d of the
hydraulic cylinder-type steam compressors. As a result, the steam
becomes an unsaturated state. Accordingly, the steam is less likely
to be condensed when fed into the steam compression chambers 8a to
8d.
[0036] The air and/or nitrogen that are mixed into the steam to be
supplied to the steam compression chambers are preferably in an
amount that is not less than 1/7 and not more than 1/3 of the
amount of the steam. Such a mixing ratio can be realized, for
example, by the following manner: adjust the pressure of the air
and/or nitrogen supplied to the flash tank 13 and/or the recovered
steam supply passage 14 to be the same as the pressure of the
steam; and adjust the flow rate of the air and/or nitrogen to
obtain a predetermined ratio. The processing apparatus shown in
FIG. 1 exerts advantageous effects that the steam is less likely to
be condensed in the steam compression chambers 8a to 8d and the
latent heat energy of the steam can be maintained easily even
without heat-insulating the steam piping.
[0037] In a case where air and/or nitrogen are supplied from the
piping 28 to the processing apparatus, it is preferred that the
pressure in reaction chambers 4a to 4d is set to be approximately
10% to 30% higher than in a case where air and/or nitrogen are not
supplied from the piping 28 to the processing apparatus. This is
for setting the partial water vapor pressure to be the same as in a
case where air and/or nitrogen are not supplied from the piping 28
to the processing apparatus.
[0038] <1. Recovery of Hydraulic Pressure>
[0039] All of the hydraulic cylinder-type steam compressors 5a to
5d operate in the same manner, and also, all of hydraulic
cylinder-type pressurized reactors 1a to 1d operate in the same
manner. Therefore, hereinafter, recovery of hydraulic pressure by a
combination of the hydraulic cylinder-type steam compressor 5a and
the hydraulic cylinder-type pressurized reactor 1a, according to
the method of hydrolyzing cellulosic biomass of the present
invention, is described based on FIGS. 2A to 2D.
[0040] (Description of FIG. 2A)
[0041] Steam is supplied to the steam compression chamber 8a of the
hydraulic cylinder-type steam compressor 5a through the steam
supply passage 14a. Accordingly, the volume of a hydraulic pressure
chamber 6a becomes minimum, and hydraulic pressure in the hydraulic
pressure chamber 6a is returned to an oil tank 26 through hydraulic
pressure return passages 19a and 19. At the time, the hydraulic
cylinder-type pressurized reactor la compresses the reaction
chamber 4a to which cellulosic biomass slurry and superheated steam
have been supplied, thereby creating a supercritical or subcritical
state and hydrolyzing the cellulosic biomass in such a state. Since
the steam is compressed by the hydraulic cylinder-type steam
compressor 5a and then further compressed in the reaction chamber
4a, the temperature and pressure of the steam are increased to the
maximum. At the time of hydrolyzing the cellulosic biomass, it is
preferred that the temperature and pressure in the reaction chamber
4a are in the ranges of 350 to 400.degree. C. and 18 to 30 MPa,
respectively. The hydrolyzing time is preferably 0.1 to 30 seconds,
and more preferably, 0.1 to 3 seconds.
[0042] A hydraulic passage 15a is a high-pressure hydraulic passage
in which the pressure is approximately 22 MPa. In the state shown
in FIG. 2A, in order to compress the reaction chamber 4a, to which
the cellulosic biomass slurry and superheated steam have been
supplied, to create a supercritical or subcritical state, a
hydraulic cylinder 3a is pushed by the hydraulic pressure of
approximately 22 MPa.
[0043] (Description of FIG. 2B)
[0044] After the hydrolysis reaction of the cellulosic biomass is
completed, the hydraulic cylinder-type pressurized reactor 1a is
quickly cooled down by reducing the pressure in the reaction
chamber 4a, and thereby further chemical reactions are stopped from
occurring. At the time, hydraulic pressure in a hydraulic pressure
chamber 2a of the hydraulic cylinder-type pressurized reactor 1a
increases. Therefore, the hydraulic pressure in the hydraulic
pressure chamber 2a is recovered through a hydraulic pressure
recovery passage 9a into the hydraulic pressure chamber 6a of the
hydraulic cylinder-type steam compressor 5a. As a result, steam in
the steam compression chamber 8a is compressed. Thus, power
necessary for compressing the steam that is supplied to the steam
compression chamber 8a in the state shown in FIG. 2A can be reduced
by utilization of the recovered hydraulic pressure.
[0045] (Description of FIG. 2C)
[0046] The steam in the steam compression chamber 8a is further
compressed, so that the steam becomes high-temperature and
high-pressure (250 to 300.degree. C., 3.9 to 8.5 MPa) superheated
steam. At the time, the slurry from which saccharides have been
produced, the temperature and pressure of which have been reduced
to those of the subcritical state or lower, is discharged from the
hydraulic cylinder-type pressurized reactor 1a to a reacted slurry
transport passage 20a. Immediately before the discharging, the
temperature and pressure of such reacted slurry are preferably in
the ranges of 150 to 300.degree. C. and 0.5 to 8.6 MPa,
respectively. Meanwhile, cellulosic biomass slurry is loaded into a
slurry feeding chamber 27 through the slurry supply passage
11a.
[0047] A hydraulic passage 16a is a low-pressure hydraulic passage
in which the pressure is approximately 2 MPa. In the state shown in
FIG. 2C, after the slurry from which saccharides have been produced
is discharged from the hydraulic cylinder-type pressurized reactor
1a to the reacted slurry transport passage 20a, the hydraulic
cylinder 3a is pushed to the left end position in the diagram by
the hydraulic pressure of appromixy 2 MPa, and thereby the volume
in the reaction chamber 4a is reduced to zero.
[0048] (Description of FIG. 2D)
[0049] The high-temperature and high-pressure superheated steam
that is discharged from the steam compression chamber 8a is
supplied to the reaction chamber 4a of the hydraulic cylinder-type
pressurized reactor 1a through a high-pressure steam supply passage
10a. At the time, the cellulosic biomass slurry in the slurry
feeding chamber 27 is concurrently supplied to the reaction chamber
4a of the hydraulic cylinder-type pressurized reactor 1a.
Meanwhile, hydraulic pressure in the hydraulic pressure chamber 2a
of the hydraulic cylinder-type pressurized reactor 1a is returned
to the oil tank 26 through hydraulic pressure return passages 17a
and 17.
[0050] The state shown in FIG. 2D is followed by the above-descried
state of FIG. 2A. Thereafter, the operations shown in FIG.
2A.fwdarw.FIG. 2B.fwdarw.FIG. 2C.fwdarw.FIG. 2D are repeated
continuously. Since the recovery of hydraulic pressure is performed
in such a continuous manner, the compression power can be
reduced.
[0051] In the present invention, surplus pressure generated at the
time of reducing the pressure in the reactor is recovered into the
steam compressor as hydraulic pressure. Therefore, the reaction
time in the reactor can be readily adjusted in accordance with the
processing object and the amount of processing. For example, the
reaction time can be adjusted for only a part of the cycle of the
reactor. Thus, freedom in changing the operating conditions is
significantly great. In this respect, the present invention is
significantly different from the inventions disclosed in Patent
Literatures 4 and 5.
[0052] <2. Recovery of Flash Steam>
[0053] Next, recovery of flash steam from reacted slurry is
described. Reacted slurry that is discharged to the reacted slurry
transport passage 20a in the state shown in FIG. 2C is moved to the
flash tank 13 through a reacted slurry transport passage 20. The
reacted slurry is flash-evaporated in the flash tank 13, so that
the pressure of the reacted slurry becomes approximately 0.1 to 1.6
MPa. Thereafter, the reacted slurry is moved from the bottom of the
flash tank 13 to an external reservoir or external fermentation
equipment by means of a pump 22.
[0054] Meanwhile, flash steam generated in the flash tank 13 is
supplied to the hydraulic cylinder-type steam compressors 5a to 5d
through the steam supply passages 14 and 14a to 14d. Then, the
above-described processing steps are repeated. If the temperature
and pressure in the flash tank 13 are lower than respective
predetermined values, then steam is supplied to the flash tank 13
from the steam generator. On the other hand, if the temperature and
pressure in the flash tank 13 are higher than the respective
predetermined values, then surplus steam is discharged to the
outside of the system.
[0055] According to the present invention, the reacted slurry can
be quickly cooled down by flash evaporation, and flash steam
generated from the reacted slurry is recovered as steam for use in
hydrolyzing the cellulosic biomass. Thus, even the latent heat of
the flash steam can be recovered. Since such steam recovery is
performed continuously, thermal efficiency is improved.
Embodiment 2
[0056] FIG. 3 is a schematic configuration diagram showing a
connection state between the hydraulic cylinder-type steam
compressor 5a and the hydraulic cylinder-type pressurized reactor
1a in another example of the processing apparatus for performing
the method of hydrolytic saccharification of cellulosic biomass
according to the present invention. The processing apparatus shown
in FIG. 3 is the same as the processing apparatus shown in FIG. 1
except that the hydraulic pressure recovery passage between the
hydraulic cylinder-type steam compressor 5a and the hydraulic
cylinder-type pressurized reactor 1a is different. In the
processing apparatus shown in FIG. 3, a hydraulic pressure recovery
passage 32 is connected to a hydraulic pressure return passage 17a,
and the hydraulic pressure recovery passage 32 is divided into four
sub-passages 32a to 32d. The sub-passages 32a to 32d are provided
with a set of respective hydraulic valves 33a to 33d.
[0057] The sub-passages 32a to 32d are connected to air chamber
passages 35a to 35d, respectively. Air chambers P.sub.1 to P.sub.4
are provided at the end of the air chamber passages 35a to 35d,
respectively. It is assumed here that pressures to be stored in the
air chambers P.sub.1 to P.sub.4 are set to 3 MPa, 8 MPa, 13 MPa,
and 18 MPa, respectively.
[0058] The air chamber passages 35a to 35d are connected to
sub-passages 36a to 36d, respectively. The sub-passages 36a to 36d
are provided with a set of respective hydraulic valves 37a to 37d.
The sub-passages 36a to 36d are connected to the hydraulic pressure
chamber 6a of the hydraulic cylinder-type steam compressor 5a via a
hydraulic pressure supply passage 36.
[0059] Although FIG. 3 shows only the connection state between the
hydraulic cylinder-type steam compressor 5a and the hydraulic
cylinder-type pressurized reactor 1a, the same connection state is
formed between the hydraulic cylinder-type steam compressors 5b to
5d and the hydraulic cylinder-type pressurized reactors 1b to 1d.
That is, the sub-passages of the hydraulic pressure recovery
passages connected to the respective hydraulic cylinder-type
pressurized reactors 1b to 1d, and the sub-passages of the
hydraulic pressure supply passages connected to the respective
hydraulic cylinder-type steam compressors 5b to 5d, are connected
to the air chamber passages 35a to 35d. The air chambers P.sub.1 to
P.sub.4 are shared by the four hydraulic cylinder-type steam
compressors and the four hydraulic cylinder-type pressurized
reactors.
[0060] Next, a hydraulic pressure recovery operation performed by
the processing apparatus shown in FIG. 3 is described. At the time
of recovering the hydraulic pressure of the hydraulic pressure
chamber 2a into the hydraulic pressure chamber 6a of the hydraulic
cylinder-type steam compressor 5a, first, a valve 34 of the
hydraulic pressure return passage 17a is closed and a valve 31 of
the hydraulic pressure recovery passage 32 is opened. At the time,
the sets of hydraulic valves 33a to 33d and 37a to 37d are in a
closed state, and a valve 38 is also in a closed state. The
hydraulic valve 33d is opened. Accordingly, a hydraulic pressure of
18 MPa is sent through the sub-passage 32d and the air chamber
passage 35d, and then stored in the air chamber P.sub.4 for
temporary storage. After the hydraulic pressure is stored, the
hydraulic valve 33d is closed.
[0061] Thereafter, the hydraulic valve 33c is opened. Accordingly,
a hydraulic pressure of 13 MPa is sent through the sub-passage 32c
and the air chamber passage 35c, and then stored in the air chamber
P.sub.3 for temporary storage. After the hydraulic pressure is
stored, the hydraulic valve 33c is closed.
[0062] Subsequently, the hydraulic valve 33b is opened.
Accordingly, a hydraulic pressure of 8 MPa is sent through the
sub-passage 32b and the air chamber passage 35b, and then stored in
the air chamber P.sub.2 for temporary storage. After the hydraulic
pressure is stored, the hydraulic valve 33b is closed.
[0063] Finally, the hydraulic valve 33a is opened. Accordingly, a
hydraulic pressure of 3 MPa is sent through the sub-passage 32a and
the air chamber passage 35a, and then stored in the air chamber
P.sub.1 for temporary storage. After the hydraulic pressure is
stored, the hydraulic valve 33a is closed. Here, the valve 31 is
also closed.
[0064] As a result of these operations, the hydraulic pressures of
3 MPa, 8 MPa, 13 MPa, and 18 MPa are temporarily stored in the air
chambers P.sub.1 to P.sub.4, respectively. Hereinafter, a
description is given of operations of supplying the hydraulic
pressures temporarily stored in the respective air chambers P.sub.1
to P.sub.4 to the hydraulic pressure chamber 6a of the hydraulic
cylinder-type steam compressor 5a.
[0065] First, the valve 38 is opened and then the hydraulic valve
37a is opened. Accordingly, the hydraulic pressure of 3 MPa stored
in the hydraulic pressure chamber P.sub.1 is supplied to the
hydraulic pressure chamber 6a through the air chamber passage 35a
and the sub-passage 36a. After the hydraulic pressure is supplied,
the hydraulic valve 37a is closed.
[0066] Thereafter, when the hydraulic valve 37b is opened, the
hydraulic pressure of 8 MPa stored in the hydraulic pressure
chamber P.sub.2 is supplied to the hydraulic pressure chamber 6a
through the air chamber passage 35b and the sub-passage 36b. After
the hydraulic pressure is supplied, the hydraulic valve 37b is
closed.
[0067] Subsequently, when the hydraulic valve 37c is opened, the
hydraulic pressure of 13 MPa stored in the hydraulic pressure
chamber P.sub.3 is supplied to the hydraulic pressure chamber 6a
through the air chamber passage 35c and the sub-passage 36c. After
the hydraulic pressure is supplied, the hydraulic valve 37c is
closed.
[0068] Finally, when the hydraulic valve 37d is opened, the
hydraulic pressure of 18 MPa stored in the hydraulic pressure
chamber P.sub.4 is supplied to the hydraulic pressure chamber 6a
through the air chamber passage 35d and the sub-passage 36d. After
the hydraulic pressure is supplied, the hydraulic valve 37d is
closed. After the hydraulic pressure supply is completed, the valve
38 is also closed, and thus one cycle of the hydraulic pressure
recovery is completed.
[0069] The sets of hydraulic valves 33a to 33d and 37a to 37d
herein are configured as, for example, hydraulic counter balance
valves and hydraulic sequence valves. Each valve has a function of
automatically opening the corresponding passage when the pressure
in the passage is within a preset pressure range, and a function of
closing the passage when the pressure in the passage becomes out of
the preset pressure range. The configurations of the sets of
hydraulic valves 33a to 33d and 37a to 37d and the air chambers
P.sub.1 to P.sub.4 shown in FIG. 3 are merely one example of
hydraulic valve sets and air chambers usable in the embodiment of
the present invention. Therefore, the configurations of hydraulic
passages, hydraulic valve sets, and air chambers are not limited to
the above.
[0070] In the state shown in FIG. 2B, the hydraulic pressure in the
hydraulic pressure chamber 2a of the hydraulic cylinder-type
pressurized reactor 1a is approximately 22 MPa, and the hydraulic
pressure in the hydraulic pressure chamber 6a of the hydraulic
cylinder-type steam compressor 5a is approximately 0.1 to 0.6 MPa.
If, in such a state, the hydraulic pressure chamber 2a and the
hydraulic pressure chamber 6a are directly connected, the flow
velocity of the oil becomes too high due to the excessive hydraulic
pressure difference. As a result, pressure loss and vibration are
caused by frictional resistance of the hydraulic piping. The
hydraulic pressure can be adjusted by installing a pressure
reducing valve on the hydraulic piping. In this case, however, the
pressure reducing valve acts as great resistance, and therefore,
pressure loss is unavoidable.
[0071] Meanwhile, the present embodiment is characterized in that
when the hydraulic pressure that is generated in the hydraulic
pressure chamber 2a of the hydraulic cylinder-type pressurized
reactor 1a is recovered into the hydraulic pressure chamber 6a of
the hydraulic cylinder-type steam compressor 5a, hydraulic
pressures are sequentially stored in the respective air chambers
P.sub.1 to P.sub.4 in descending order of the pressure level, and
then the hydraulic pressures are sequentially supplied from the
respective air chambers P.sub.1 to P.sub.4 to the hydraulic
pressure chamber 6a in ascending order of the pressure level. In
this manner, the hydraulic pressures are temporarily stored once in
the respective air chambers, and then the stored hydraulic
pressures are sequentially recovered in ascending order of the
pressure level. Accordingly, even if the hydraulic pressure to be
recovered is high, an excessive hydraulic pressure difference can
be eliminated, and vibration of the piping can be prevented while
preventing loss of the hydraulic pressure.
[0072] (Conventional Art)
[0073] FIG. 4 is a schematic configuration diagram showing an
example of a conventional processing apparatus for performing a
method of hydrolytic saccharification of cellulosic biomass. The
method performed by the conventional processing apparatus is the
same as the method of hydrolytic saccharification of cellulosic
biomass according to the present invention in terms of that
cellulosic biomass slurry and superheated steam are compressed by a
hydraulic cylinder-type pressurized reactor into a supercritical or
subcritical state and the cellulosic biomass is hydrolyzed in such
a state. However, the conventional processing apparatus is not
configured such that superheated steam supplied from a steam
generator (not shown) such as a boiler is recompressed by a steam
compressor and then supplied to the hydraulic cylinder-type
pressurized reactor. Moreover, the conventional processing
apparatus is not configured to recover flash steam from reacted
slurry.
[0074] Hereinafter, the method of hydrolyzing cellulosic biomass
that is performed by the processing apparatus shown in FIG. 4 is
described. Cellulosic biomass slurry is supplied to a reaction
chamber 46 of a hydraulic cylinder-type pressurized reactor 43
through a slurry supply passage 41. Meanwhile, superheated steam
from a steam generator is supplied to the reaction chamber 46 of
the hydraulic cylinder-type pressurized reactor 43 through a
high-pressure steam supply passage 42. A hydraulic cylinder 45 of
the hydraulic cylinder-type pressurized reactor 43 is operated by
hydraulic pressure supplied from a hydraulic passage 47. Oil in a
pressure oil tank 56 is supplied to the hydraulic passage 47 by
means of a hydraulic pump 49.
[0075] The hydraulic cylinder-type pressurized reactor 43
compresses the reaction chamber 46, to which the cellulosic biomass
slurry and high-pressure steam (i.e., superheated steam) have been
supplied, to create a supercritical or subcritical state, and
hydrolyzes the cellulosic biomass in such a state. After the
hydrolysis reaction of the cellulosic biomass is completed, the
pressure in the reaction chamber 46 is reduced and thereby the
reaction chamber 46 is quickly cooled down, so that further
chemical reactions are stopped from occurring. At the time, oil in
a hydraulic pressure chamber 44 is returned through a hydraulic
pressure return passage 48 to the oil tank 56 which is open to the
atmosphere. Therefore, surplus pressure (surplus hydraulic
pressure) cannot be recovered from the hydraulic cylinder-type
pressurized reactor 43 as compression power for compressing the
superheated steam.
[0076] The reacted slurry is supplied to a flash tank 51 through a
reacted slurry transport passage 50. Flash steam generated in the
flash tank 51 is discharged from the tank 51 through a flash steam
exhaust passage 52, and then discharged by a heat exchanger 53 as
condensation water. The discharged condensation water is reusable
as a source of soft water used by the steam generator. In this
case, however, the latent heat of the flash steam cannot be
recovered. The reacted slurry is, after being cooled down, removed
from the flash tank 51 to the outside through a saccharified
solution passage 54 by means of a pump 55.
[0077] As described above, the method of hydrolyzing cellulosic
biomass according to the present invention makes it possible to
recover surplus pressure at the time of reducing the pressure in
the reactor, thereby reducing compression power, and to recover
latent heat through cyclic use of flash steam, thereby improving
thermal efficiency. Moreover, in the method of hydrolyzing
cellulosic biomass according to the present invention, surplus
pressure generated at the time of reducing the pressure in the
reactor is used, in the form of hydraulic pressure, as the
compression power of the steam compressor. Thus, unlike the
inventions disclosed in Patent Literatures 4 and 5, there is a lot
of freedom in the operating timing of the reactor and the operating
timing of the steam compressor. The method according to the present
invention makes is possible to operate both the reactor and steam
compressor in conjunction with each other in such a manner that the
reactor and steam compressor are operated at their respective
optimal timings.
[0078] From the foregoing description, numerous modifications and
other embodiments of the present invention are obvious to one
skilled in the art. Therefore, the foregoing description should be
interpreted only as an example and is provided for the purpose of
teaching the best mode for carrying out the present invention to
one skilled in the art. The structural and/or functional details
may be substantially altered without departing from the spirit of
the present invention.
INDUSTRIAL APPLICABILITY
[0079] The method and apparatus of hydrolyzing cellulosic biomass
according to the present invention are useful in the fields of
bioenergy as a method and apparatus for use in hydrolyzing
cellulosic biomass to produce saccharides.
Reference Signs List
[0080] 1a to 1d: hydraulic cylinder-type pressurized reactor
[0081] 2a to 2d: hydraulic pressure chamber
[0082] 3a to 3d: hydraulic cylinder
[0083] 4a to 4d: reaction chamber
[0084] 5a to 5d: hydraulic cylinder-type steam compressor
[0085] 6a to 6d: hydraulic pressure chamber
[0086] 7a to 7d: hydraulic cylinder
[0087] 8a to 8d: steam compression chamber
[0088] 9a to 9d: hydraulic pressure recovery passage
[0089] 10a to 10d: high-pressure steam supply passage
[0090] 11, 11a to 11d: slurry supply passage
[0091] 12: steam supply passage
[0092] 13: flash tank
[0093] 14, 14a to 14d: steam supply passage
[0094] 15, 15a to 15d: hydraulic passage
[0095] 16, 16a to 16d: hydraulic passage
[0096] 17, 17a to 17d: hydraulic pressure return passage
[0097] 18, 18a to 18d: hydraulic passage
[0098] 19, 19a to 19d: hydraulic pressure return passage
[0099] 20, 20a to 20d: reacted slurry transport passage
[0100] 21: saccharified solution passage
[0101] 22: pump
[0102] 23, 24, 25: hydraulic pump
[0103] 26: oil tank
[0104] 27: slurry feeding chamber
[0105] 28, 28a, 28b: piping
[0106] 31, 34, 38: valve
[0107] 32: hydraulic pressure recovery passage
[0108] 32a to 32d: hydraulic pressure recovery passage
(sub-passage)
[0109] 33a to 33d: set of hydraulic valves
[0110] 35a to 35d: air chamber passage
[0111] 36: hydraulic pressure recovery passage
[0112] 36a to 36d: hydraulic pressure supply passage
(sub-passage)
[0113] 37a to 37d: set of hydraulic valves
[0114] 41: slurry supply passage
[0115] 42: high-pressure steam supply passage
[0116] 43: hydraulic cylinder-type pressurized reactor
[0117] 44: hydraulic pressure chamber
[0118] 45: hydraulic cylinder
[0119] 46: reaction chamber
[0120] 47: hydraulic passage
[0121] 48: hydraulic pressure return passage
[0122] 49: hydraulic pump
[0123] 50: reacted slurry transport passage
[0124] 51: flash tank
[0125] 52: flash steam exhaust passage
[0126] 53: heat exchanger
[0127] 54: saccharified solution passage
[0128] 55: pump
[0129] P.sub.1 to P.sub.4: air chamber
* * * * *