Title of Invention

METHOD FOR CRYSTALLIZATION OF ORGANIC COMPOUND THROUGH ADIABATIC COOLING

Abstract The present invention provides a method for adiabatic cooling type crystallization of organic compound. The method comprises carrying out adiabatic cooling and evaporation operation of a coolant in a crystallizer 20 for a mixture solution of a target organic compound containing the coolant; taking out crystal slurry produced by the operation from the crystallizer 20; pressurizing evaporated vapor to a pressure higher than the operation pressure in the crystallizer 20 by a compressor 30, introducing the vapor to an absorption condenser 10; cooling for condensation the mixture solution of organic compound and the evaporated vapor that has been pressurized while allowing them to contact each other in the absorption condenser 10; and introducing this absorption condensate to the crystallizer 20.
Full Text BACKGROUND OF THE INVENTION
Field of the Invention
The present invention relates to a method for adiabatic
cooling type crystallization of organic compound and an
apparatus therefore, and more particularly to a method and an
apparatus suitable for obtaining paraxylene crystal.
Description of the Related Art
Separation and purification of a certain kind of isomer
mixture are difficult in distillation operation because boiling
points of components constituting the mixture are close to each
other. However, there are many cases where melting points are
largely different depending on the difference in molecular
structures, and therefore, separation by crystallization
operation is often effective.
There are methods of extractive and adductive
crystallization in which a solvent-agent (extractant,
additive) is added to a two-component eutectic system or a
multi-component eutectic system as a third component; however,
these are disadvantageous to recover the solvent-agent.


In this regard, a method in which a liquified gas component
is used as a coolant is advantageous because its recovery is
easy.
The present inventors have found that it is effective to
carry out crystallization operation, with the use of propane
(propene, ethylene, carbon dioxide, ammonia, or the like) as
a direct injecting coolant, for a multi-component eutectic
system such as xylene mixture
(m-xylene+o-xylene+ethylbenzene+p-xylene system) that is a raw
material for a typical p-xylene production in a petrochemical
industrial process or a xylene mixture
(m-xylene+o-xylene+p-xylene system) after isomerization
reaction.
In this case, it is possible to carry out the
crystallization operation in a jacket type crystallizer;
however the crystallization is necessary to be carried out by
cooling p-xylene in the multi-component eutectic system to about
-30 degrees C to -60 degrees C. Therefore, it is required to
provide the crystallizer with a cooling surface scraper
mechanics and a refrigiration unit by which the evaporated
coolant from the jacket is compressed by a compressor, for
example, under a high pressure of 20 atmospheres, followed by
allowing this to be liquified and circulated to the jacket.


Using such a crystallizer results in not only an increase
in power cost of the compressor but also increases in facility
cost and maintenance cost because the crystallizer has to be
provided with a cooling surface scraper mechanics that requires
complex and frequent maintenance.
On the other hand, another system in which a heat pump
is used is conceivable (Patent document 1: Japanese Patent
Application Laid-Open Publication No. 1992-327542), but the
system is not necessarily suitable in view of facility cost to
construct the heat pump.
SUMMARY OF THE INVENTION
Main objects of the present invention are to provide
a method for adiabatic cooling type crystallization of organic
compound and an apparatus therefore in which running cost
(including maintenance cost) and facility cost can be reduced.
Other objects of the present invention are to provide
a method and an apparatus suitable for crystallization of
p-xylene.
The present invention to solve the above problems is
carried out as follows.



A method for adiabatic cooling type crystallization of
organic compound comprising:
carrying out adiabatic cooling, as for crystallization
operation of target organic compound and evaporation operation
of a coolant which is directly introduced in crystallizer for
a mixture solution of a target organic compound containing the
coolant;
taking out crystal slurry produced by the operation from
the crystallizer;
pressurizing evaporated vapor to a pressure higher than
the operation pressure in the crystallizer by a compressor,
introducing the pressurized coolant vapor to an absorption
condenser, removing the heat of absorption and condensation,
cooling the mixture solution of organic compound and the
evaporated coolant vapor that has been pressurized, while
allowing them to contact each other in the absorption condenser;
and
introducing this absorption condensate to the
crystallizer.
(Advantageous effect)
When the adiabatic cooling and the evaporation operation
of the coolant are carried out for the mixture solution of the
target organic compound containing the coolant in the
crystallizer, heat of crystallization is taken away in


association with evaporation of substantially only the liquid
coolant component, and crystal is crystallized. The evaporated
vapor is pressurized to a pressure higher than the operation
pressure in the crystallizer by the compressor and introduced
to the absorption condenser for condensation. The reason why
the evaporated vapor is pressurized to a pressure higher than
the operation pressure in the crystallizer by the compressor
is that a temperature difference for the condensation is
generated as in the case of common refrigeration cycle, by
pressurizing the evaporated vapor by the compressor. In the
absorption condenser, since the evaporated vapor is brought into
contact with the mixture solution of organic compound having
a lower atmospheric pressure, the boiling point rises, thereby
raising the temperature at which absorption and condensation
can take place. Accordingly, a smaller degree of
pressurization suffices the need, and a smaller energy input
from outside suffices the need for the condensation.
Continuous crystallization operation can be carried out
by introducing condensate liquid from the absorption condenser
to the crystallizer. Taking crystallization of p-xylene as an
example, propane is used as a coolant, the pressure in the
crystallizer is, for example, normal atmospheric pressure, and
the pressure in the absorption condenser is, for example, about
eight atmospheric pressure by means of pressurization by the
compressor. The crystal slurry produced in the crystallizer


is taken out, separated into a crystal portion and mother liquid
by a solid-liquid separation means. The crystal portion
becomes a product as it is or after being purified by a
purification means as necessary to enhance the purity. Since
the target component remains in the mother liquid, it can be
sent back to the crystallizer.
According to the above operation, crystallization
operation is possible without constructing the crystallizer as
a pressure resistant container. When at least a compressor and
an absorption condenser are included as other necessary
apparatuses, crystallization operation can be carried out, and
therefore, an expensive structure installed with a
refrigeration unit that was used in the prior art is not
necessary, thus giving rise to an economical apparatus in view
of entire system cost and running cost.

* *
The method for adiabatic cooling type crystallization
of organic compound according to claim 1, where the crystal
slurry taken out from the crystallizer is subjected to
solid-liquid separation, and the separated mother liquid is sent
back to the absorption condenser.
(Advantageous effect)
In the absorption condenser, not only is the mixture


solution of organic compound supplied and brought into contact
with the evaporated vapor that has been pressurized but also
the crystal slurry taken out from the crystallizer is subjected
to solid-liquid separation by a centrifuge, a liquid cyclone
that is preferred in view of apparatus cost, or the like, and
the separated mother liquid is sent back to the absorption
condenser, thereby allowing it to come in contact with the
evaporated vapor that has been pressurized . Which mode is to
be selected can be determined depending on the kind of a target
organic compound, concentration of the target organic compound
in a feed mixture solution and operation conditions.
Facilities and steps for the solid-liquid separation are not
limited; however, for example, a centrifuge, a filter, a melt
purification column, and a piston type or screw type wash column
can be included.

The method for adiabatic cooling type crystallization
of organic compound according to claim 1, where the operation
pressure in the crystallizer is vacuum or equal to or lower than
four atmospheric pressure.
(Advantageous effect)
As to the operation pressure in the crystallizer
(evaporation pressure) , the operation is preferably carried out
at around normal atmospheric pressure and at most at four


atmospheric pressure when a pressure resistance property
required for the crystallizer and the like, the separation
method of produced crystal, and the apparatus are taken into
consideration.

The method for adiabatic cooling type crystallization
of organic compound according to claim 1, where the
concentration of the coolant in the absorption condensate
introduced from the absorption condenser to the crystallizer
is set to from 1 to 70%.
(Advantageous effect)
When the concentration of the coolant in the absorption
condensate becomes higher, the crystallization point becomes
lower, and the vapor pressure also becomes lower. When the
concentration of the coolant in the absorption condensate
becomes lower, the vapor pressure becomes lower in relation to
the partial pressure. Accordingly, the highest point of the
vapor pressure exists. When the concentration of the coolant
in the absorption condensate is from 1 to 70%, the operation
around the highest point of the vapor pressure is possible.

The method for adiabatic cooling type crystallization
of organic compound according to claim 1, where the mixture


solution of organic compound is a xylene mixture containing
paraxylene, from which paraxylene crystal is obtained.
(Advantageous effect)
The method is advantageous to obtain paraxylene
crystal.

The method for adiabatic cooling type crystallization
of organic compound according to claim 1, where the mixture
solution of organic compound is a hexane mixture containing
cyclohexane, from which cyclohexane crystal is obtained.
(Advantageous effect)
The method is advantageous to obtain cyclohexane
crystal.

An apparatus for adiabatic cooling type crystallization
of organic compound comprising:
a crystallizer in which adiabatic cooling,
crystallization and evaporation operation of a coolant are
carried out for a mixture solution of a target organic compound
containing the coolant;
a means to take out crystal slurry produced by the
operation from the crystallizer;


Fig. 1 is a flow sheet of a basic embodiment;
Fig. 2 is a flow sheet of another embodiment; and
Fig. 3 is a solid-liquid equilibrium diagram of a
eutectic composition of propane-benzene-cyclohexane system.
DETAILED DESCRIPTION
Hereinafter, exemplary embodiments of the present
invention will be explained in detail.

Fig. 1 represents a basic embodiment, which includes
an absorption condenser 10, a crystallizer 20, a compressor 30,
and a solid-liquid separation means 40.
A mixture solution 1 of a target organic compound
containing a coolant (target liquid for crystallization
operation, for example, a liquid of multi-component eutectic
mixture containing p-xylene and its isomer) is introduced to
the absorption condenser 10 and allowed to absorb coolant vapor
(for example, propane) here to be condensed, making a
homogeneous liquid mixed with the coolant. The liquid is
introduced to the crystallizer 20 via a piping path 61 from a
temporary storage tank 10A for absorption condensate, and
adiabatic cooling and evaporation operation of the coolant is
carried out for the condensed liquid containing the coolant in
the crystallizer 20.


Crystal slurry produced by this operation is taken out
from the crystallizer 20 by a pump 62 and separated into a flow
of crystal portion Cr and a flow of mother liquid Mo by the
solid-liquid separation means 40 such as centrifuge or liquid
cyclone.
The evaporated vapor in the crystallizer 20 is allowed
to pass a piping path 63, pressurized to a pressure higher than
the operation pressure in the crystallizer 20 by the compressor
30, and introduced to the absorption condenser 10. While
bringing the mixture solution of organic compound (mixture
solution 1) into contact with the evaporated vapor that has been
pressurized in the absorption condenser 10, absorption and
condensation are carried out by cooling with cooling heat that
a cooling medium 2 (for example, cooling water in coolling column
or brine in freezer) has, and this absorption condensate is
introduced to the crystallizer 20.
When adiabatic evaporation operation for the liquid
coolant component is carried out, in the crystallizer 20, for
the mixture solution of the target organic compound containing
the liquid coolant component, crystallization heat is taken away
in association with the evaporation of the liquid coolant
component, and crystal is crystallized. The evaporated vapor
is pressurized to a pressure higher than the operation pressure


in the crystallizer 20 by the compressor 30 and introduced to
the absorption condenser 10 to be subjected to absorption and
condensation.
A temperature difference between the crystallizer 20
and the absorption condenser 10 that allows recondensation of
the coolant at a temperature much higher than the operation
temperature of the crystallizer 20 is secured by means of
pressurization by the compressor 30.
In the absorption condenser 10, the evaporated vapor
is brought into contact with the solution of the organic compound
having high boiling points, and therefore the boiling point
rises, thereby raising the temperature at which absorption and
condensation can take place. Accordingly, a smaller energy
input from outside suffices the need for absorption and
condensation. It is possible to carry out continuous
crystallization operation by introducing the absorption
condensate in the absorption condenser 10 to the crystallizer
20. Taking crystallization of p-xylene as an example, propane
is used as a coolant, the pressure in the crystallizer 20 is,
for example, normal atmospheric pressure, and the pressure in
the absorption condenser 10 is, for example, about eight
atmospheric pressure by means of pressurization by the
compressor 30. The crystal slurry produced in the crystallizer
20 is taken out, separated into the flow of crystal portion Cr


and the flow of mother liquid Mo by a solid-liquid separation
means. The flow of crystal portion Cr becomes a product as it
is or after purification by a purification means as necessary
as described later to enhance the purity. Since the target
component remains in the flow of mother liquid Mo, part of the
flow of mother liquid Mo can be sent back to the crystallizer
20 via a piping path 64 in order to enhance the recovery rate
of the crystal of the target component.
According to the operation, crystallization operation
is possible without constructing the crystallizer 20 as a
pressure resistant container. When at least the compressor 30
and the absorption condenser 10 are included as necessary
apparatuses, crystallization operation can be carried out, and
therefore, an expensive structure installed with a
refrigeration system that was used in the prior art is not
necessary, thus giving rise to an economical apparatus in view
of entire system cost and running cost.

Fig. 2 represents a second embodiment. The crystal
slurry taken out from the crystallizer 20 is subjected to
solid-liquid separation by the solid-liquid separation means
40, and the separated flow of mother liquid Mo is sent back to
the absorption condenser 10 via the piping path 64. The coolant
in the portion discharged to the outside of the system in a state


that the coolant is dissolved in the filtrate obtained by the
solid-liquid separation means 40 can be recovered by the
distillation column in the subsequent stage or supplied to a
suction means of the compressor 30 as make-up (refer to Fig.
1, too).
For solid-liquid separation, a centrifuge, a filter,
a cyclone, or the like can be used.
The initial mixture solution 1 of organic compound may
be directly supplied to the crystallizer 20.
Explanation of a method for crystallization>
Taking a benzene-cyclohexane system as an example, the
method for crystallization is explained.
In common production in chemical industry, cyclohexane
is produced by hydrogenation of benzene.
C6H6+3H2 -> C6H12
In this hydrogenation reaction, the following
impurities are produced by side reactions.
Methylcyclopentane
n-hexane
n-pentane
methylcyclohexane
In addition to these, toluene and paraffins contained
in the raw material benzene are included.
In such a case, what is the most difficult in obtaining


cyclohexane with high purity is that it becomes almost
impossible to separate cyclohexane by distillation when
unreacted benzene is contained. The boiling point of benzene
at normal atmospheric pressure is 80.75 degrees C, and that of
cyclohexane is 80.16 degrees C. The difference between them
is only 0.59 degree C. Further, the lowest azeotropic point
(77.62 degrees C) is around 54mol% of cyclohexane.
On the other hand, as is clear from the solid-liquid
equilibrium diagram of a eutectic composition of
propane-benzene-cyclohexane system shown in Fig. 3, a method
of separation and purification by crystallization can be adopted
when cyclohexane with high purity is desired to be obtained.
In this method, it becomes possible to remove impurities such
as methylcyclopentane contained together in a small amount at
the same time.
In other words, in the phase diagram, a solid-liquid
equilibrium line of the two-component system consisting of
cyclohexane and benzene can be obtained. The content of
impurities in a very small amount only slightly lowers the
crystallization point curve, and there is no large substantial
difference. When it is intended here that a mixed raw material
rich in cyclohexane is cooled to crystallize cyclohexane,
crystallization starts when the temperature reaches the
solid-liquid line on the left side. Next, in the method for


adiabatic cooling using propane, when a supply liquid and
propane are mixed and cooling is started by releasing the
pressure, crossing the solid-liquid equilibrium line (the line
is drawn as component without propane) of the three-component
system having added propane takes place. When cooling the
liquid along the line to near the eutectic point, crystal of
cyclohexane is crystallized, and this crystal is separated from
the mother liquid.
Such operation is continuously carried out in the
facility structure according to the present invention. The
mother liquid separated from the cyclohexane crystal is
subjected to propane removal, mixed with the raw material, and
fed back. Note that a mixed liquid system of benzene and
cyclohexane is a eutectic system in the range of all
concentrations. The crystallization point of pure benzene is
5.5 degrees C and that of cyclohexane is 5.7 degrees C.
From the explanation of this principle, it will be
obvious that cyclohexane crystal can be obtained from a eutectic
composition of propane-benzene-cyclohexane system. Further,
according to the present invention, it will be also clear that
a low cost crystallization process is provided for their
separation.



The above embodiments are examples in which one
crystallizer is used. However, the present invention also aims
at a structure provided with a plurality of crystallizers. In
a facility provided with a plurality of crystallizers, crystal
slurry in a crystallizer in a previous stage is introduced to
a crystallizer in the subsequent stage, followed by carrying
out further crystallization.
In this mode, a structure in which one compressor is
provided, and evaporated vapor from the crystallizer in each
stage is collectively introduced to the compressor and
pressurized, followed by being introduced to the absorption
condenser provided to a crystallizer in the final stage is more
preferable than a case where a compressor is provided to each
crystallizer in every stage.
(Example 1)
Hereinafter, the effects of the present invention are
made clear by showing examples.
In the following example, crystallization was carried
out by the process shown in Fig. 1. An vertical crystallizer
(300 millimeter diameter x 1.5 meter height, slurry hold-up
capacity of 25 liters) was used as the crystallizer 20, and a
horizontal tube type absorption condenser was used for the
absorption condenser 10, and a centrifuge was used as the
solid-liquid separation means 40. The numerical number 30


represents a compressor for vapor, and 10A represents a
temporary storage tank for absorption condensate.
A raw material of xylene mixture having 80 to 90 %
paraxylene concentration at normal temperature was supplied to
the absorption condenser 10 at a rate of 15 to 25 kg/hr and
condensed at about 30 degrees C while being brought into contact
with and mixed with the vapor pressurized to 0.2 to 0.7
megapascal (MPa) by passing through the compressor 30 from the
crystallizer 20. The obtained condensed liquid was a solution
of xylene mixture containing propane at a concentration of 10

to 30%. This solution was introduced to the crystallizer 20
being run at -1O to 0 degree C under normal atmospheric pressure
for crystallization. The paraxylene crystal slurry obtained
by the crystallization was supplied to the centrifuge 40 from
the crystallizer 20. As the result, xylene crystal could be
obtained at 4 to 7 kg/hr. The filtrate that was the solution
of xylene mixture containing propane was discharged to the
outside of the system. The propane in the portion discharged
to the outside of the system in a state that the propane was
dissolved in the filtrate was supplied to the suction means of
the compressor 30 as make-up. The concentration of paraxylene
in the filtrate was 60 to 80%.
(Example 2)
In the example 1, the raw material of xylene mixture
having 70 to 80 % paraxylene concentration at normal temperature


obtained as a filtrate from the centrifuge 40 was supplied to
the absorption condenser 10 at a rate of 15 to 25 kg/hr and
condensed at about 30 degrees C while being brought into contact
with and mixed with the vapor pressurized to 0.2 to 0.7 MPa by
passing through the compressor 30 from the crystallizer 20. The
obtained condensed liquid was a solution of xylene mixture
containing propane at a concentration of 10 to 30%. This
solution was introduced to the crystallizer 20 being run at -20
to -5 degrees C under normal atmospheric pressure for
crystallization. Paraxylene crystal slurry obtained by the
crystallization was supplied to the centrifuge 40 from the
crystallizer 20. As the result, xylene crystal could be
obtained at 4 to 7 kg/hr. The filtrate that was the solution
of xylene mixture containing propane was discharged to the
outside of the system. The propane in the portion discharged
to the outside of the system in a state that the propane was
dissolved in the filtrate was supplied to the suction means of
the compressor 30 as make-up. The concentration of paraxylene
in the filtrate was 50 to 70%.


WE CLAIM:
1. A method for adiabatic cooling type crystallization
of organic compound comprising:
carrying out adiabatic cooling at -20°C to 0°C, as
for crystallization operation of target paraxylene and
evaporation operation of propane which is directly
introduced in a crystallizer for a xylene mixture containing
the target paraxylene along with the—propane;
taking out crystal slurry produced by the operation
from the crystallizer;
pressurizing evaporated propane vapor by a
compressor, introducing the pressurized evaporated propane
vapor to an absorption condenser;
setting an operation pressure in the crystallizer be
in a range from around normal atmospheric pressure to 4
atmospheric pressure and setting a pressure of the
evaporated propane vapor pressurized by the compressor to be
higher than the operation pressure in the crystallizer;
in the absorption condenser, cooling, by cooling
water in a cooling column, the xylene mixture containing the
paraxylene and the pressurized propane vapor, while allowing
the xylene mixture containing the paraxylene and the
pressurized propane vapor to contact each other so as to
condense the propane vapor, thus producing absorption
condensate wherein the concentration of propane is set to
from 1% to 70%; and
introducing this absorption condensate to the


crystallizer so as to obtain paraxylene crystal from the
crystal slurry produced in the crystallizer.
2. The method for adiabatic cooling type crystallization
of organic compound as claimed in claim 1, wherein the
crystal slurry taken out from the crystallizer is subjected
to solid-liquid separation, and the separated mother liquid
is sent back to the absorption condenser.


ABSTRACT

METHOD FOR CRYSTALLIZATION OF ORGANIC COMPOUND
THROUGH ADIABATIC COOLING
The present invention provides a method for adiabatic cooling type crystallization of
organic compound.
The method comprises carrying out adiabatic cooling and evaporation
operation of a coolant in a crystallizer 20 for a mixture solution of a target organic
compound containing the coolant; taking out crystal slurry produced by the operation
from the crystallizer 20; pressurizing evaporated vapor to a pressure higher than the
operation pressure in the crystallizer 20 by a compressor 30, introducing the vapor
to an absorption condenser 10; cooling for condensation the mixture solution of
organic compound and the evaporated vapor that has been pressurized while
allowing them to contact each other in the absorption condenser 10; and introducing
this absorption condensate to the crystallizer 20.

Documents:

03125-kolnp-2007-abstract.pdf

03125-kolnp-2007-claims.pdf

03125-kolnp-2007-correspondence others.pdf

03125-kolnp-2007-description complete.pdf

03125-kolnp-2007-drawings.pdf

03125-kolnp-2007-form 1.pdf

03125-kolnp-2007-form 3.pdf

03125-kolnp-2007-form 5.pdf

03125-kolnp-2007-international publication.pdf

03125-kolnp-2007-international search report.pdf

03125-kolnp-2007-pct request form.pdf

3125-KOLNP-2007-(15-12-2011)-ABSTRACT.pdf

3125-KOLNP-2007-(15-12-2011)-AMANDED CLAIMS.pdf

3125-KOLNP-2007-(15-12-2011)-DESCRIPTION (COMPLETE).pdf

3125-KOLNP-2007-(15-12-2011)-DRAWINGS.pdf

3125-KOLNP-2007-(15-12-2011)-EXAMINATION REPORT REPLY RECEIVED.pdf

3125-KOLNP-2007-(15-12-2011)-FORM-1.pdf

3125-KOLNP-2007-(15-12-2011)-FORM-2.pdf

3125-KOLNP-2007-(15-12-2011)-OTHERS.pdf

3125-KOLNP-2007-(16-05-2012)-ABSTRACT.pdf

3125-KOLNP-2007-(16-05-2012)-AMANDED CLAIMS.pdf

3125-KOLNP-2007-(16-05-2012)-AMANDED PAGES OF SPECIFICATION.pdf

3125-KOLNP-2007-(16-05-2012)-CORRESPONDENCE.pdf

3125-KOLNP-2007-(16-05-2012)-DESCRIPTION (COMPLETE).pdf

3125-KOLNP-2007-(16-05-2012)-DRAWINGS.pdf

3125-KOLNP-2007-(16-05-2012)-FORM-1.pdf

3125-KOLNP-2007-(16-05-2012)-FORM-2.pdf

3125-KOLNP-2007-(16-05-2012)-FORM-3.pdf

3125-KOLNP-2007-(16-05-2012)-OTHERS.pdf

3125-KOLNP-2007-(25-07-2012)-ABSTRACT.pdf

3125-KOLNP-2007-(25-07-2012)-ANNEXURE TO FORM 3.pdf

3125-KOLNP-2007-(25-07-2012)-CORRESPONDENCE.pdf

3125-KOLNP-2007-(25-07-2012)-FORM-1.pdf

3125-KOLNP-2007-(25-07-2012)-FORM-2.pdf

3125-KOLNP-2007-(25-07-2012)-OTHERS.pdf

3125-KOLNP-2007-ASSIGNMENT-1.1.pdf

3125-KOLNP-2007-ASSIGNMENT.pdf

3125-KOLNP-2007-CORRESPONDENCE OTHERS 1.1.pdf

3125-KOLNP-2007-CORRESPONDENCE.pdf

3125-KOLNP-2007-EXAMINATION REPORT.pdf

3125-KOLNP-2007-FORM 18-1.1.pdf

3125-kolnp-2007-form 18.pdf

3125-KOLNP-2007-FORM 3-1.1.pdf

3125-KOLNP-2007-FORM 5.pdf

3125-KOLNP-2007-GPA-1.1.pdf

3125-KOLNP-2007-GPA.pdf

3125-KOLNP-2007-GRANTED-ABSTRACT.pdf

3125-KOLNP-2007-GRANTED-CLAIMS.pdf

3125-KOLNP-2007-GRANTED-DESCRIPTION (COMPLETE).pdf

3125-KOLNP-2007-GRANTED-DRAWINGS.pdf

3125-KOLNP-2007-GRANTED-FORM 1.pdf

3125-KOLNP-2007-GRANTED-FORM 2.pdf

3125-KOLNP-2007-GRANTED-SPECIFICATION.pdf

3125-KOLNP-2007-INTERNATIONAL PUBLICATION.pdf

3125-KOLNP-2007-INTERNATIONAL SEARCH REPORT.pdf

3125-KOLNP-2007-OTHERS.pdf

3125-KOLNP-2007-PCT REQUEST FORM.pdf

3125-KOLNP-2007-PRIORITY DOCUMENT.pdf

3125-KOLNP-2007-REPLY TO EXAMINATION REPORT.pdf

3125-KOLNP-2007-TRANSLATED COPY OF PRIORITY DOCUMENT.pdf

abstract-03125-kolnp-2007.jpg


Patent Number 254209
Indian Patent Application Number 3125/KOLNP/2007
PG Journal Number 40/2012
Publication Date 05-Oct-2012
Grant Date 03-Oct-2012
Date of Filing 24-Aug-2007
Name of Patentee TSUKISHIMA KIKAI CO., LTD.
Applicant Address 17-15 TSUKUDA 2-CHOME, CHUO-KU TOKYO
Inventors:
# Inventor's Name Inventor's Address
1 ISHII KIWAMU C/O TSUKISHIMA KIKAI CO. LTD. 17-15 TSUKUDA 2-CHOME, CHUO-KU TOKYO 1040051
2 TAKEGAMI KEIZO C/O TSUKISHIMA KIKAI CO. LTD. 17-15 TSUKUDA 2-CHOME, CHUO-KU TOKYO 1040051
3 WAKAYAMA JUNJI C/O TSUKISHIMA KIKAI CO. LTD. 17-15 TSUKUDA 2-CHOME, CHUO-KU TOKYO 1040051
PCT International Classification Number B01D 9/02,C07C 13/18
PCT International Application Number PCT/JP2006/304329
PCT International Filing date 2006-03-07
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 2005-100172 2005-03-30 Japan