Title of Invention

"A LIQUID-LIQUID EXTRACTING METHOD OF A PARA TOLUIC ACID FROM WASTEWATER"

Abstract A liquid-liquid extracting method of a para toluic acid from wastewater, which is generated from a terephthalic acid plant (1), with para-xylene, characterized by flowing the wastewater and the para-xylene into a static mixer (2,4) having a structure in which the wastewater and the para-xylene are mixed, so as to mix the wastewater and the para-xylene with each other; supplying a mixed liquid to a static settling separator (5)while decelerating the liquid by gravity; standing the mixed liquid to liquid-liquid separate; and wherein the static settling separator (3, 5) has a partition plate as high as 10 to 70% of the height of the container; liquid-liquid separated heavy liquid is drained from a lower portion of a compartment opposite to a compartment, to which the mixed liquid is supplied; and liquid-liquid separated light liquid is drained from an upper portion of the compartment opposite to the compartment, to which the mixed liquid is supplied.
Full Text The present invention relates to a liquid-liquid extracting method of a para toluic acid from wastewater.
TECHNICAL FIELD
The present invention relates to a method of extracting a target ingredient from large liquid flow stream, for example, over 50 t/hr of wastewater.
BACKGROUND ART
In general, when wastewater contains a low concentration of useful substance, it is not economically profitable to recover the useful substance, whereby the wastewater is disposed by an activated sludge process. For example, even though a large amount of para toluic acid, which is a reaction product, is contained in the wastewater generated from a device that produces high-purity terephthalic acid, the concentration of the para toluic acid is low, and thus the wastewater is disposed by the activated sludge process.
However, the activated sludge process does not only bring a loss of the useful substance, but also consumes a great amount of energy such as electricity or the like for the operation. In addition, the activated sludge
process causes smell. As the size of the device increases like the device that produces terephthalic acid, and thus the amount of wastewater augments, it is required to remove and recover the useful substance from the wastewater from viewpoints of economy as well as global environment.
As a method of recovering the useful substance from the wastewater, for example, Japanese Patent No. 2899927 discloses a method of extracting para toluic acid contained in the wastewater, which is generated from the terephthalic acid-producing device, with para-xylene. In the above method, since para-xylene, which is a raw material of terephthalic acid, is used as extractant, it is advantageous that a recycling process of the extractant is not necessary. However, since a conventional extracting device is very expensive, the above method does not have economic benefit.
Methods of extracting useful substance from wastewater are well known. For example, the Handbook of Chemical Engineering, 5th edition (edited by the society of Chemical Engineers, Japan) discloses various methods in section 11.5.
However, for example, in the case of a mixer-settler extractor disclosed in section 11.5.1 of the Handbook,

the structure becomes complex and the price rises when the extractor is used for multi-stage extraction, whereby a tower-like extracting device is used in the multi-stage extraction. However, in the case of a countercurrent differential extraction tower disclosed in section 11.5.2 of the Handbook, a simple-structured extraction tower generates drift, and thus the size of the extraction tower is hard to increase, whereby the extraction tower is rarely used in the industrial field. If the extraction tower is operated in a pulsating mode or the like in order to overcome the above disadvantages, the drift can be suppressed, however, the structure becomes complex and the price rises. In addition, in the case of a non-agitating type multi-stage extraction tower disclosed in section 11.5.3 of the Handbook, even though the structure is simple, the operating range is narrow, and the operating flexibility lacks. In order to overcome the above disadvantages, an agitating type multi-stage extraction tower, disclosed in section 11.5.4 of the Handbook, or the like is devised, however, the structure is complex and the price is high. As described above, in the tower-like extractors, the structure becomes complex and the price rises when the drift is prevented, and the operating range is widened.

If a highly efficient and low price extracting device exists, not only can dilute useful substance contained in the wastewater or the like be recovered, but also the wastewater can be purified, whereby water can be recycled,
However, it is difficult to perform commercially the method of extracting para toluic acid contained in the wastewater, which is generated from the terephthalic acid-producing device, with para-xylene, which is disclosed in JP-A-2899927, 'because there is no low price extracting device.
DISCLOSURE OF INVENTION
An advantage of the invention is to provide a method, with which large liquid flow stream of liquid-liquid extraction is performed efficiently and easily in a wide operating range, and particularly, to provide a preferable method to extracting useful substance from over 50 t/hr of wastewater, which is generated from a device that produces, industrially important, high-purity terephthalic acid.
Even though the invention is composed of operations such as mixing and static settling separation, similar to an extracting operation in the related art, the invention

provides an extracting method suitable to dispose large liquid flow stream of wastewater.
That is, the invention relates to a liquid-liquid extracting method including steps of flowing wastewater and extractant, which is used to extract a target ingredient from the wastewater, into a pipe having a structure in which the wastewater and the extractant are mixed, so as to mix the wastewater and the extractant with each other; supplying a mixed liquid to a container while decelerating the liquid by gravity; and standing so that the mixed liquid is liquid-liquid separated. It is preferable that the mixed liquid be supplied from a bottom of the container while being decelerated by gravity.
In addition, the invention relates to a liquid-liquid extracting method including steps of flowing wastewater and extractant, which is used to extract a target ingredient from the wastewater, into a pipe having a structure in which the wastewater and the extractant are mixed, so as to mix the wastewater and the extractant with each other; supplying a mixed liquid to a container from a bottom thereof; and standing so that the mixed liquid is liquid-liquid separated.

It is preferable that the pipe be composed of a static mixer. In addition, it is preferable that the pipe is vertically arranged, the mixed liquid be flowed from top to bottom in a case in which light liquid is a dispersed phase, and the mixed liquid be flowed from bottom to top in a case in which heavy liquid is a dispersed phase. In this case, the light liquid means a low-density liquid, generally an organic liquid, and the heavy liquid means a high-density liquid, generally water.
As a method of decelerating the inflow of the mixed liquid, a method of supplying the mixed liquid through the bottom of the container to decelerate the inflow of the mixed liquid by using gravity is preferably used, since the above method does not disturb the flow of the mixed liquid in the container in which the mixed liquid is static settling-separated. As a decelerating method using gravity, it is possible to inject the mixed liquid in the opposite direction of gravity from the bottom of the container or to inject the mixed liquid toward the bottom of the container and then reverse the flow of the mixed liquid at the bottom of the container. In any case, it is desirable to check whether the inflow of the mixed liquid is decelerated within a short period with no

disturbance in the container by the computerized analysis of the flowing state of the mixed liquid.
Furthermore, the invention provides a liquid-liquid extracting method, in which the container is pressurized, and the wastewater and the extractant are drained by using the pressure of the container, or a liquid-liquid extracting method, in which the container is fully filled with water, and does not have a liquid level control device that controls an interface between gas phase and liquid phase, and pressure control device.
It is preferable that, after static settling separation, the wastewater and the extractant be drained respectively by flow control, which is cascade-controlled on the basis of the amount of the wastewater or the extractant flowed into the container.
Still furthermore, the invention provides a liquid-liquid extracting method, in which the container has a partition plate as high as 10 to 70% of the height of the container; liquid-liquid extracted heavy liquid (water phase) is drained through a lower portion of a compartment opposite to a compartment, to which the mixed liquid is supplied; and liquid-liquid extracted light liquid (organic phase) is drained through an upper

portion of the compartment opposite to the compartment, to which the mixed liquid is supplied.
By combining two or more stages of the above liquid-liquid extracting method, multi-stage extraction can be performed. As the wastewater in the above liquid-liquid extracting method, wastewater of a terephthalic acid plant can be used.
BRIEF DESCRIPTION OF DRAWINGS
Fig. 1 is an explanatory view showing an embodiment of the invention.
1 terephthalic acid plant
2 static mixer
3 static settling separator
4 static mixer
5 static settling separator
6 pump
7 pump
8 flow controller
9 flow controller
10 flow controller
11 flow controller
SI terephthalic acid plant wastewater discharging stream

52 wastewater supplying stream to the static mixer
of the first stage
53 para-xylene supplying stream
54 para-xylene supplying stream to the flow
controller of the static mixer of the first stage
55 para-xylene supplying stream to the static mixer
of the first stage
56 supplying stream to the static settling
separator of the first stage
57 para-xylene outflow stream from the static
settling separator of the first stage
58 para-xylene returning stream from the static
settling separator of the first stage
59 wastewater outflow stream from the static
settling separator of the first stage

510 para-xylene supplying stream to the flow
controller of the static mixer of the second stage
511 para-xylene supplying stream to the static mixer
of the second stage
512 supplying stream to the static settling
separator of the second stage
513 para-xylene outflow stream from the static
settling separator of the second stage

58 para-xylene returning stream from the static
settling separator of the second stage
59 wastewater outflow stream from the static
settling separator of the second stage
BEST MODE FOR CARRYING OUT THE INVENTION The invention can provide a liquid-liquid extracting method suitable to treat the large liquid flow stream of wastewater by, for example, flowing feed (raw material to be solvent-extracted, specifically wastewater) and extractant into a pipe having a structure in which the flows of the feed and the extractant are mixed, and then mixing the feed and the extractant with each other; supplying a mixed liquid through a lower portion of a static settling separator fully filled with water and under pressurization; and draining the feed and the extractant by using the pressure of the static settling separator under pressurization on the basis of the flow of the feed or the extractant.
The feed and the extractant are mixed by an agitator in a conventional mixer settler extractor. However, multi-stage extraction requires a plurality of expensive agitating devices and agitating containers, which is not economical. In addition, since a tower-like extractor

without a mechanical agitator cannot mix the feed and the extractant sufficiently, the extraction efficiency is low. In the invention, since a pipe having a structure in which the flows of the feed and the extractant are mixed is used, the feed and the extractant are efficiently mixed by a simple device.
For example, a static mixer can be used as the pipe having a structure in which the flows of the feed and the extractant are mixed. Even though an extracting operation using the static mixer is well known, the multi-stage extraction requires a pump for each stage due to the pressure loss at the static mixer. In the invention, since a static settling separator is pressurized, liquid is drained by using pressure, not pump. Accordingly, the problem in which a pump is required for each stage is solved. In addition, the invention solves a problem in which a pressure control device is additionally required for pressurization, by fully filling the static settling separator with water.
In a conventional static settling separator having gas phase and interface between liquid phase and gas phase, two liquid level control devices are required. In addition, the liquid should be held in the static settling separator for a longer time than the time

required for liquid-liquid separation to control liquid level. In the invention, since the feed and the extractant are drained on the basis of the flow of supplied feed and extractant, the liquid level control device for controlling the interface between two liquid phases is not required. Furthermore, in the invention, the liquid level control device for controlling the interface between gas phase and liquid phase is not required by fully filling the static settling separator with water.
Since the liquid level control is not required in the invention, the liquid can be held in the static settling separator only for a time required for the liquid-liquid separation,-, that is, the liquid does not have to be held for a longer time for the liquid level control. In general, it takes over 10 minutes to control the liquid level. If the liquid level control is not required by using the invention, for example, in the case of para-xylene and water systems, which can be easily separated, if the flow is not generated, para-xylene and water systems can be separated within one minute. Therefore, the size of the static settling separator can be as small as the static settling separator can secure time to decelerate the flow of .the feed and the extractant.

Specifically, nonuse of the liquid level control devices as described above can be achieved by the cascade control of the inflow amount and outflow amount of the feed and the extractant, which are flown into and from the container. For example, when the extractant is para-xylene and the feed is wastewater, the same amount of para-xylene as the flow of supplied para-xylene is drained from the static settling separator by the cascade-control, and the wastewater is drained as much as the container can be fully filled with water. Since the wastewater is the heavy liquid, the wastewater is drained as much as the container can be fully filled with- water----^ if a seal operation is carried out to install a drainpipe at a position higher than that of the container.
When the flow of the wastewater is controlled, the same amount of wastewater as. the flow of supplied wastewater is drained from the static settling separator by the cascade-control, and the para-xylene is overflowed from the upper portion of the container, whereby the wastewater is drained as much as the container can be fully filled with water. Since the inflow amount is not completely equal to the outflow amount, it is required to finely tune for the wastewater not to flow into the para-xylene and vice versa. However, once tuned, the

wastewater and the para-xylene can be drained stably without mixture.
The invention seeks to minimize the size of the static settling separator by supplying the mixed liquid through the lower portion of the static settling separator so as to decelerate the supplying speed thereof by using gravity. In addition, it is also possible to put a filling substance in the supplying pipe to decelerate the supplying speed thereof. However, in the case of a large-scaled device, it is also possible to use a pipe with a sufficiently large diameter and/or to supply the mixed liquid through a plurality of pipes for the purpose of increasing the cross sectional area of the supplying pipe.
In addition, in the invention, since the mixed liquid is supplied through the lower portion of the static settling separator and a partition plate is provided between a supply opening and an outflow opening for the heavy liquid, the flowing direction of the heavy liquid is completely reversed so as to maximize time required for the route, in which the feed and the extractant are separated. It is preferable that the partition plate be as high as 10 to 70% of the height of the container. As described above, when the mixed liquid is supplied from

the bottom of the container, it is possible to use inertial force as well as gravity. Accordingly, when the flow speed of the heavy liquid dominates the separation due to the fact the flow of the heavy liquid is larger than that of the light liquid, the invention becomes more useful particularly. Meanwhile, in the invention, the light liquid means a low-density liquid of the liquid to be mixed, generally an organic liquid, and the heavy liquid means a high-density liquid of the liquid to be mixed, generally water.
In the invention, the feed and the extractant are mixed by a simple-structured pipe, as described above, and a particularly structured static settling separator is not used. Accordingly, it is possible to perform a stable extraction in a wide operating range. Even though the minimum limit of the operating range is a point, at which mixture in the pipe becomes insufficient due to the reduction of the flow speed, if the pipe is disposed vertically, preferably perpendicularly, the operating range can be widened by flowing the mixed liquid from top to bottom in a case in which the light liquid is a dispersed phase, and from bottom to top in a case in which the heavy liquid is a dispersed phase. The maximum limit of the operating range depends on the separating

ability of the static settling separator. However, since the time to reduce the flow speed of the mixed liquid in the static settling separator reaches the limit ahead of the time to liquid-liquid extract the mixed liquid in the static settling separator, the operating range can be widened by simple methods such as by enlarging the diameter of the static settling separator that supplies the mixed liquid to the static settling separator and/or by supplying the mixed liquid through a plurality of pipes. Meanwhile, the operating range means a flow range of the light liquid and the heavy liquid, and the maximum and minimum limits of the operating xange mean the maximum and minimum flows, respectively.
The invention can be applied to, for example, the wastewater disposal in terephthalic acid production. The application example will be described below.
Para-xylene is oxidized with the air by using cobalt compound, manganese compound and bromine compound as catalyst in acetate solvent at the reaction pressure of 0.4 to 5 MPa-G and the reaction temperature of 160 to 260°C so as to produce crude terephthalic acid. Main impurities in the crude terephthalic acid are 500 to 5000 ppm by weight of 4-carboxybenzaldehyde, which is an

oxidation intermediate, and 100 to 1000 ppm by weight of para toluic acid.
The obtained crude terephthalic acid is dissolved in water by raising the temperature up to 225°C or more, preferably 250 to 310°C, under the pressure of 5 MPa-G or more, preferably 7 to 9 MPa-G. In this case, the concentration of the terephthalic acid in the water is adjusted to be in the range of 10 to 40% by weight, preferably 20 to 35% by weight.
And then, the terephthalic acid solution is contacted with a catalyst, for example, palladium, in the presence of hydrogen so as to reduce the oxidation intermediate 4-carboxybenzaaldehyde, which is the main impurity in the crude terephthalic acid, into para toulic acid, which is easily removed by crystallization. After that, the terephthalic acid is crystallized by one or multi stages, preferably three to seven stages, of pressure reduction and then solid-liquid separated so as to produce high-purity terephthalic acid.
The pressure of wastewater generated from the above high-purity terephthalic acid producing process and para-xylene serving as the extractant, is raised up to 0.15 MPa-G or more, preferably 0.3 to 1.0 MPa-G, and then the wastewater and the para-xylene are flowed into and mixed

in a static mixer. The mixing ratio is 5 to 70 parts by weight, preferably 10 to 40 parts by weight, of the para-xylene to 100 parts by weight of the wastewater. The number of reversion in the static mixer is in the range of 2 to 30, preferably 5 to 15.
After that, the mixed liquid from the static mixer is supplied through the lower portion of a compartment •partitioned by a partition plate of the static settling separator having the partition plate at the central portion under the pressure of 0.1 MPa-G or more, preferably 0.25 to 9.95 MPa-G, and the para-xylene and the wastewater are separated with each other. The same amount of the separated para-xylene as that of the supplied para-xylene is drained through the upper portion of the other compartment of the static settling separator by flow control, and the wastewater is drained through the lower portion. The drained wastewater is mixed with the para-xylene again by the static mixer and supplied through the lower portion of the compartment partitioned by the partition plate of the static settling separator having the partition plate at the central portion under the pressure of 0.05 MPa-G or more, preferably 0.2 to 9.9 MPa-G, and the para-xylene and the wastewater are separated with each other.

The wastewater, from which impurities are extracted by the para-xylene twice as described above, is recycled as water for purifying the crude terephthalic acid after the para-xylene in the mixed and dissolved portions is removed and recovered by steam-stripping. In some cases, the extraction by para-xylene alone cannot remove impurities that influence, .bad.effect on the quality of high-purity terephthalic acid. In these cases, since the amount of impurities is extremely small, the impurities are removed by activated carbon, membrane separation or the like, and then the wastewater is recycled as water for purifying the crude terephthalic acid. In addition, the para-xylene drained through the upper portion of the separator is used as raw material for producing crude terephthalic acid.
[Example]
Even though an example of the invention will be described below, the invention is not limited to the following example.
Fig. 1 is an explanatory view showing an embodiment of the invention. Wastewater from a terephthalic acid plant 1 flowed through a wastewater-discharging stream SI, and the pressure of the wastewater was raised up to 0.6 MPa-G by a pump 6. After that, the wastewater was mixed

with para-xylene from a supplying stream S5 by a static mixer 2. The para-xylene from the supplying stream S5 flowed in a supplying stream S3, and the pressure of the para-xylene was raised up to 0.7 MPa-G by a pump 7. After that, the flow of the para-xylene was controlled so as to be one part by weight with respect to four parts by weight of the wastewater by a flow controller 10. The static mixer 2 was manufactured by the Noritake Co., Limited and had 12 flowing direction-reversing elements and 15 seconds of holding time.
A liquid mixed by the static mixer 2 flowed through a supplying stream S6 and was supplied through the lower portion of a static settling separator 3. Liquid-liquid extracted para-xylene flowed through an outflow stream S7, and the flow of the para-xylene was controlled by a flow controller 8. After that, the para-xylene was drained and then send to the terephthalic acid plant 1 from a returning stream S8, and then the para-xylene was used as raw material of terephthalic acid. The flow controller 8 was cascade-controlled to have the same flow as that of the flow controller 10. The pressure of the static settling separator 3 was 0.55 MPa-G, and the holding time thereof was 3 minutes.

Liquid-liquid extracted wastewater flowed through an outflow stream S9 from the lower portion of the static settling separator 3 and then was mixed with para-xylene from a supplying stream Sll by a static mixer 4. The outflow stream S9 was once arranged at a position higher than that of the static settling separator 3 in order to make the static settling separator 3 fully filled with water. The para-xylene from a supplying stream Sll flowed through a supplying stream S3, and the pressure of the para-xylene was raised up to 0.7 MPa-G by the pump 7. After that, the flow of the para-xylene was controlled so as to be one part by weight with respect to four parts by weight of the wastewater by a flow controller 11. The static mixer 4 was manufactured by the Noritake Co., Limited and had 12 flowing direction-reversing elements and 15 seconds of holding time.
A liquid mixed by the static mixer 4 flowed through a supplying stream S12 and was supplied through the lower portion of a static settling separator 5. Liquid-liquid extracted para-xylene flowed through an outflow stream S13, and the flow of the para-xylene was controlled by a flow controller 9. After that, the para-xylene was drained and then send to the terephthalic acid plant 1 from a returning stream S14, and then the para-xylene was

used as raw material of terephthalic acid. The flow controller 9 was cascade-controlled to have the same flow as that of the flow controller 11. The pressure of the static settling separator 5 was 0.5 MPa-G, and the holding time thereof was 3 minutes.
The wastewater drained from an outflow stream S15 at the lower portion of the static settling separator 5 was steam-stripped so as to remove and recover the remaining para-xylene, and then impurities that could not be removed by the para-xylene were removed by RO membrane. After that, the wastewater was recycled as water for purifying crude terephthalic acid. The outflow stream S15 was once arranged at a position higher than that of the static settling separator 5 in order to make the static settling separator 5 fully filled with water.
As described above, 90% by weight of para toulic acid contained in the wastewater from the terephthalic acid plant 1 could be recovered by a device having no particular agitator or filling substance within extremely short holding time of 6 minutes 30 seconds.
The invention provides a method, with which large liquid flow stream of liquid-liquid extraction is performed efficiently and easily in a wide operating range.

The invention provides a practical method particularly when useful substance is extracted from wastewater, which is large liquid flow stream but contains a low concentration of useful substance, for example, over 50 t/hr of wastewater generated from a device that produces high-purity terephthalic acid, thereby being disposed in the related art due to small economic benefit.













We Claim:
1. A liquid-liquid extracting method of a para toluic acid from wastewater, which is
generated from a terephthalic acid plant (1), with para-xylene, characterized by
flowing the wastewater and the para-xylene into a static mixer (2,4) having a structure in which the wastewater and the para-xylene are mixed, so as to mix the wastewater and the para-xylene with each other;
supplying a mixed liquid to a static settling separator (5)while decelerating the
liquid by gravity;
standing the mixed liquid to liquid-liquid separate; and
wherein the static settling separator (3, 5) has a partition plate as high as 10 to 70% of the height of the container; liquid-liquid separated heavy liquid is drained from a lower portion of a compartment opposite to a compartment, to which the mixed liquid is supplied; and liquid-liquid separated light liquid is drained from an upper portion of the compartment opposite to the compartment, to which the mixed liquid is supplied.
2. The liquid-liquid extracting method as claimed in claim 1,
wherein the mixed liquid is supplied from a bottom of the static settling separator (5) while being decelerated by gravity.
3. The liquid-liquid extracting method as claimed in any one of claims 1 to 2,
wherein the static mixer (2,4) is vertically arranged, the mixed liquid is flowed
from top to bottom in a case in which light liquid is a dispersed phase, and the mixed liquid is flowed from bottom to top in a case in which heavy liquid is a dispersed phase.
4. The liquid-liquid extracting method as claimed in any one of claims 1 to 3,
wherein the static settling separator (3,5) is pressurized, and the wastewater and
the para-xylene are drained by using the pressure of the static settling separator (3,5).

5. The liquid-liquid extracting method as claimed in any one of claims 1 to 4,
wherein the static settling separator (3,5) is fully filled with water, and is without
a liquid level control device that controls an interface between gas phase and liquid phase, and pressure control device.
6. The liquid-liquid extracting method as claimed in any one of claims 1 to 5,
wherein, after static settling separation, the wastewater and the para-xylene are
drained respectively by flow control, which is cascade-controlled on the basis of the amount of the wastewater or the para-xylene flowed into the static settling separator
(3,5).
7. A liquid-liquid extracting method, performing multistage extraction by
combining two or more stages of the liquid-liquid extracting method as claimed in any
one of claims 1 to 6.

Documents:

87-del-2006-Abstract-(19-05-2011).pdf

87-DEL-2006-Abstract-(26-06-2009).pdf

87-del-2006-abstract.pdf

87-del-2006-Claims-(12-03-2010).pdf

87-del-2006-Claims-(19-05-2011).pdf

87-DEL-2006-Claims-(26-06-2009).pdf

87-del-2006-Claims-(29-03-2010).pdf

87-del-2006-claims.pdf

87-DEL-2006-Correspondence Others-(31-05-2011).pdf

87-DEL-2006-Correspondence-Others- (03-03-2010).pdf

87-DEL-2006-Correspondence-Others-(03-03-2010).pdf

87-del-2006-Correspondence-Others-(12-03-2010).pdf

87-del-2006-Correspondence-Others-(19-05-2011).pdf

87-DEL-2006-Correspondence-Others-(23-03-2010).pdf

87-DEL-2006-Correspondence-Others-(26-06-2009).pdf

87-del-2006-Correspondence-Others-(29-03-2010).pdf

87-del-2006-correspondence-others-1.pdf

87-del-2006-correspondence-others.pdf

87-del-2006-Description (Complete)-(19-05-2011).pdf

87-DEL-2006-Description (Complete)-(26-06-2009).pdf

87-del-2006-description (complete).pdf

87-DEL-2006-Drawings-(26-06-2009).pdf

87-del-2006-drawings.pdf

87-del-2006-Form-1-(19-05-2011).pdf

87-DEL-2006-Form-1-(26-06-2009).pdf

87-del-2006-form-1.pdf

87-del-2006-form-18.pdf

87-del-2006-Form-2-(19-05-2011).pdf

87-del-2006-form-2.pdf

87-del-2006-Form-3-(12-03-2010).pdf

87-DEL-2006-Form-3-(26-06-2009).pdf

87-del-2006-Form-3-(29-03-2010).pdf

87-DEL-2006-Form-3-(31-05-2011).pdf

87-del-2006-form-3.pdf

87-DEL-2006-Form-5-(26-06-2009).pdf

87-del-2006-form-5.pdf

87-DEL-2006-GPA-(26-06-2009).pdf

87-del-2006-gpa.pdf

87-DEL-2006-Petition-137-(26-06-2009).pdf

87-DEL-2006-Petition-138-(26-06-2009).pdf


Patent Number 248505
Indian Patent Application Number 87/DEL/2006
PG Journal Number 29/2011
Publication Date 22-Jul-2011
Grant Date 20-Jul-2011
Date of Filing 12-Jan-2006
Name of Patentee MITSUI CHEMICALS, INC.
Applicant Address 5-2, HIGASHI-SHIMBASHI, 1-CHOME, MINATO-KU, TOKYO, JAPAN.
Inventors:
# Inventor's Name Inventor's Address
1 FUJIMASA NAKAO C/O MITSUI CHEMICALS, INC., 6-1-2, WAKI, WAKICHO, KUGA-GUN, YAMAGUCHI, JAPAN.
2 YOSHIAKI UEMURA C/O MITSUI CHEMICALS, INC., 6-1-2, WAKI, WAKICHO, KUGA-GUN, YAMAGUCHI, JAPAN.
3 TAKANOBU MURAI C/O MITSUI CHEMICALS, INC., 6-1-2, WAKI, WAKICHO, KUGA-GUN, YAMAGUCHI, JAPAN.
4 DAISUKE YAMAMOTO C/O MITSUI CHEMICALS, INC., 6-1-2, WAKI, WAKICHO, KUGA-GUN, YAMAGUCHI, JAPAN.
PCT International Classification Number B29C 43/00
PCT International Application Number N/A
PCT International Filing date
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 2005-008528 2005-01-17 Japan