CN107779221A - A kind of method that n-alkane improves octane number in separation gasoline - Google Patents
A kind of method that n-alkane improves octane number in separation gasoline Download PDFInfo
- Publication number
- CN107779221A CN107779221A CN201711047651.6A CN201711047651A CN107779221A CN 107779221 A CN107779221 A CN 107779221A CN 201711047651 A CN201711047651 A CN 201711047651A CN 107779221 A CN107779221 A CN 107779221A
- Authority
- CN
- China
- Prior art keywords
- oil
- product
- phase product
- gasoline
- alkane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/20—Organic compounds not containing metal atoms
- C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
Abstract
The method that n-alkane improves octane number in gasoline is separated the invention discloses a kind of.Methods described comprises the following steps：Gasoline is through the isolated light component oil of weight component and heavy constituent oil；Heavy constituent oil mixes with enveloping agent solution carries out complex reaction, filtered to obtain liquid-phase product and solids product；Liquid-phase product is through washing to obtain oil phase product；Light component oil obtains product oil with oil phase product mix, that is, improves octane number.The present invention is significantly improved using urea and the more existing independent effect for using urea complexation separating normal alkane of effect of mixture any in thiocarbamide, biuret and biruea as the n-alkane in complexing agent Separation by Complexation gasoline.The inventive method complexing agent and n-alkane carry out complex reaction below room temperature, are advantageous to improve the separating effect of n-alkane.The present invention is applicable not only to catalytically cracked gasoline, applies also for the separation process of other gasoline, straight-run diesel oil, isomery diesel oil and other positive isohydrocarbon compositions containing more than C6 normal paraffin components.
Description
Technical field
The present invention relates to a kind of method for improving octane number, and in particular to n-alkane improves in one kind separation gasoline
The method of octane number.
Background technology
Octane number is a kind of numerical indication for weighing gasoline Ulva Pertusa burning capacity in cylinder, and its value is high to represent anti-
Quick-fried property is good.High-octane method is put forward at present and generally uses secondary operation technique, such as hydroforming, isomerization, alkylation, etherificate
, can also to improve gasoline pungent by adding RONA as octane number is not still up to standard after secondary operation Deng to improve gasoline label
The Mn class RONAs such as alkane value, conventional additives MMT, CMT, NMT, but highest lifting RON2~2.8 unit, or pass through
The antiknock component (such as MTBE/ETBE) that reconciles improves octane number, but cost is high, addition up to 15%, and lifting amplitude is
RON3 unit or so.
Urea dewaxing is to form complex compound using urea molecule and the n-alkane in diesel oil, then complex separation is gone out into liquid
Wax, realize the separation of n-alkane in diesel oil.Urea dewaxing has the advantages that equipment is simple, energy consumption is low, dewaxing effect is good.Patent
CN102504867A discloses a kind of dry method dewaxing technique, by separating the wax in 600SN base oils, produce condensation point less than-
50 DEG C, the good dewaxing oil product of low temperature flow.
Patent CN105567320A and CN105505458A disclose a kind of production method of high-octane rating low-sulphur oil, pass through
De- n-alkane handles to obtain the gasoline products of non-n-alkane content 90~100%, but in terms of analysis result, its sulfur content knot
Fruit is still higher, and octane number RON results also only improve 3 points.
F- T synthesis is by CO and H2The intermediate products mistake based on paraffin hydrocarbon is formed under the conditions of catalyst and appropriate reaction
Journey, gasoline products can be made through processes such as catalytic cracking in Fischer-Tropsch intermediate products, n-alkane is mainly C5 in the gasoline products
~C12 n-alkane.Because n-alkane octane number is low (normal heptane RON=0, more than C7 n-alkane RON is negative), pass through
Complexing agent forms complex separation with n-alkane in gasoline, can separate the n-alkane of low octane rating, so as to carry
The octane number of high product oil, but because catalytically cracked gasoline boiling range is relatively low, Conventional urea complexing method can not be by n-alkane point
From.
The content of the invention
It is an object of the invention to provide a kind of method for separating n-alkane raising octane number in gasoline, more particularly to
The separation method of n-alkane suitable for separation gasoline.
The method provided by the present invention for improving octane number, comprises the following steps：
(1) gasoline is through the isolated light component oil of weight component and heavy constituent oil；
(2) the heavy constituent oil mixes with enveloping agent solution, carries out complex reaction, filtered to obtain liquid-phase product and solid phase
Product；
(3) liquid-phase product obtains oil phase product through washing；
The oil phase product is the heavy constituent oil for removing n-alkane；
(4) light component is oily obtains product oil with the oil phase product mix, that is, improves octane number.
In above-mentioned method, in step (1), the gasoline can be catalytically cracked gasoline, and boiling range is 30~220 DEG C；
The temperature of the weight component separation is 70~120 DEG C.
In above-mentioned method, in step (2), complexing agent that the enveloping agent solution uses for it is following 1) or 2)：
1) thiocarbamide, biuret or biruea；
2) urea and mixture any in thiocarbamide, biuret and biruea；
The mass ratio of the urea and the thiocarbamide, the biuret or the biruea is 1：1~5, preferably 1：1；
Solvent in the enveloping agent solution is ethanol, mass fraction is 95% ethanol water, methanol, propyl alcohol, fourth
Alcohol, acetone or butanone.
In above-mentioned method, in step (2), the mass ratio of complexing agent and heavy constituent oil in the enveloping agent solution
For 1~5：1~5, preferably 1：1；
The temperature of the complex reaction is -30~15 DEG C, such as -10~0 DEG C, -10 DEG C or 0 DEG C.
In above-mentioned method, in step (3), the quality that the washing adds water is the 1~3 of the liquid-phase product quality
Times.
In above-mentioned method, methods described is also including the step of solids product is handled as follows：
Be dissolved in water the solids product, is isolated to aqueous phase and oil phase product A；
The oil phase product A obtains oil phase product B and rinse water through washing,
The oil phase product B is the n-alkane isolated, and aromatisation or cracked stock can be further used as, for making
Standby aromatic hydrocarbons or low-carbon alkene product.
In above-mentioned method, the aqueous phase is isolated to the complexing agent.
In above-mentioned method, the quality for dissolving the solids product addition water is 1~3 times of the solids product quality；
The temperature of the dissolving is 20~80 DEG C；
The quality that the washing adds water is 1~3 times of the oil phase product A mass.
In above-mentioned method, the aqueous solution after washing needs separating treatment, and the separating treatment can take rectifying or liquid separation, institute
It can be conventional distillation, extracting rectifying and/or azeotropic distillation to state rectifying.
The heavy constituent oil RON obtained by the inventive method can improve 5~20 units, and product oil RON can improve 3~10
Individual unit.
The inventive method has advantages below：
The inventive method is to separate the n-alkane of low octane rating in gasoline component, and separation process is stable, separating effect
Good, raw material is easy to get, and energy consumption is low, and equipment is simple, and reagent, solvent used in separation process are repeatable to be utilized, environmentally friendly.
The inventive method is using urea with the mixture of any one in thiocarbamide, biuret and biruea as complexing agent network
The more existing independent effect for using urea complexation separating normal alkane of effect for closing the n-alkane in separation gasoline has significantly
Improve.
In the inventive method, complexing agent and n-alkane carry out complex reaction below room temperature, are advantageous to improve N-alkanes
The separating effect of hydrocarbon.
The present invention is applicable not only to catalytically cracked gasoline, applies also for other gasoline, straight-run diesel oil, isomery diesel oil and other
The separation process of positive isohydrocarbon composition containing more than C6 normal paraffin components.
Brief description of the drawings
Fig. 1 is the flow chart that the present invention separates the separation method of n-alkane in gasoline using urea.
Embodiment
Experimental method used in following embodiments is conventional method unless otherwise specified.
Material used, reagent etc., unless otherwise specified, are commercially obtained in following embodiments.
Embodiment 1,
Flow carries out purifying recovery to catalytically cracked gasoline as shown in Figure 1, by 100kg/h catalytically cracked gasolines 101 through step
Rapid 1 cuts into the oily 102 and 50kg heavy constituents oil 103 of 50kg light components by 100 DEG C；Heavy constituent oil 103 is added to through step 2
50kg/h urea and thiocarbamide (urea：Thiocarbamide=1:1, mass ratio) in ethanol solution, gradually it is cooled to -10 DEG C and stirs
To suspension 104；Suspension 104 obtains solids product 105 and liquid-phase product 110 through vacuum filter 3；Solids product 105 is through step
Rapid 4 are dissolved in water to obtain oil phase product 106 and rinse water 107, and the quality of added water is 100~150kg/h；Rinse water 107 can
Isolated complexing agent and water；Oil phase product 106 is further washed through step 5, and the quality of water is 100~150kg/h, obtains oil
Phase product 108 (n-alkane removed) and rinse water 109；The liquid-phase product 110 obtained after vacuum filter 3 is through step 6
Washing, the quality of water is 100~150kg/h, obtains oil phase product 111 (the heavy constituent oil of removing n-alkane) and rinse water
112, rinse water 109 and 112 can further handle to obtain absolute ethyl alcohol and water；Oil phase product 111 and light component oil 102 are through step 7
The gasoline products 113 of octane number are improved after mixing.
The analysis of components and octane number of each major product in the processing procedure of 1 embodiment of table 1
From the data of table 1：With urea and thiocarbamide (1:1) it is complexing agent, after separating normal alkane, liquid-phase product (weight
Component oil) RON is by 65.6 raisings to 85.1, and 19.5 units of raising, product oil RON is by 87.2 raisings to 94.6, RON raising
7.4 units.
Embodiment 2,
Flow carries out purifying recovery to catalytically cracked gasoline as shown in Figure 1, by 100kg/h catalytically cracked gasolines 101 through step
Rapid 1 cuts into light component oil 102 and heavy constituent oil 103 by 70 DEG C；Heavy constituent oil 103 is added to urea and thiocarbamide (urine through step 2
Element:Thiocarbamide=1:1, mass ratio) alcohol saturated solution in, the gross mass of urea and thiocarbamide and the mass ratio of heavy constituent oil 103
For 1:1, gradually it is cooled to -10 DEG C and stirring obtains suspension 104；Suspension 104 obtains solids product 105 through vacuum filter 3
With liquid-phase product 110；Solids product 105 is dissolved in water to obtain oil phase product 106 and rinse water 107, the matter of added water through step 4
Measure as 100~150kg/h；Rinse water 107 is separable to obtain complexing agent and water；Oil phase product 106 is further washed through step 5,
The quality of water is 100~150kg/h, obtains oil phase product 108 (n-alkane removed) and rinse water 109；Through vacuum mistake
The liquid-phase product 110 obtained after filter 3 is washed through step 6, and the quality of water is 100~150kg/h, obtains (the removing of oil phase product 111
The heavy constituent oil of n-alkane) and rinse water 112.
The analysis of components and octane number of each major product in the processing procedure of 2 embodiment of table 2
From the data of table 2：With urea and thiocarbamide (1:1) it is complexing agent, after separating normal alkane, liquid-phase product (weight
Component oil) RON improves to 100.5, RON by 86.4 and improves 14 units.
Embodiment 3,
Flow carries out purifying recovery to catalytically cracked gasoline as shown in Figure 1, by 100kg/h catalytically cracked gasolines 101 through step
Rapid 1 cuts into light component oil 102 and heavy constituent oil 103 by 100 DEG C；Heavy constituent oil 103 is added to urea and biuret through step 2
(urea：Biuret=1:1, mass ratio) alcohol saturated solution in, gross mass and the heavy constituent oil 103 of urea and biuret
Mass ratio is 1:1, gradually it is cooled to 0 DEG C and stirring obtains suspension 104；Suspension 104 obtains solids product through vacuum filter 3
105 and liquid-phase product 110；Solids product 105 is dissolved in water to obtain oil phase product 106 and rinse water 107, added water through step 4
Quality be 100~150kg/h；Rinse water 107 is separable to obtain urea and water；Oil phase product 106 is through the further water of step 5
Wash, the quality of water is 100~150kg/h, obtains oil phase product 108 (n-alkane removed) and rinse water 109；Through vacuum
The liquid-phase product 110 obtained after filter 23 is washed through step 6, and the quality of water is 100~150kg/h, and it is (de- to obtain oil phase product 111
Except the heavy constituent oil of n-alkane) and rinse water 112.
The analysis of components and octane number of each major product in the processing procedure of 3 embodiment of table 3
From the data of table 3：With urea and biuret (1：1) it is complexing agent, after separating normal alkane, liquid-phase product
(heavy constituent oil) RON is improved to 81.9, RON by 69.8 and is improved 12.1 units.
Comparative example 1,
Flow carries out purifying recovery to catalytically cracked gasoline as shown in Figure 1, and 100kg/h catalytically cracked gasolines 101 is direct
It is added to through step 2 in the ethanol solution of urea, is gradually cooled to 20 DEG C and stirring obtains suspension 104；Suspension 104 is through true
Empty filter 23 obtains solids product 105 and liquid-phase product 110；The liquid-phase product 110 obtained after vacuum filter 3 is washed through step 6
Obtain oil phase product 111 and rinse water 112.
The analysis of components and octane number of each major product in the processing procedure of 4 comparative example of table 1
Comparative example 2,
Flow carries out purifying recovery to catalytically cracked gasoline as shown in Figure 1, by 100kg/h catalytically cracked gasolines 101 through step
Rapid 1 cuts into light component oil 102 and heavy constituent oil 103 by 120 DEG C；The ethanol that heavy constituent oil 103 is added to urea through step 2 is molten
In liquid, gradually it is cooled to 20 DEG C and stirring obtains suspension 104；Suspension 104 obtains the He of solids product 105 through vacuum filter 3
Liquid-phase product 110；The liquid-phase product 110 obtained after vacuum filter 3 obtains oil phase product 111 and rinse water through step 6 washing
112。
The analysis of components and octane number of each major product in the processing procedure of 5 comparative example of table 2
It can be seen that to add thiocarbamide in complexing agent urea and reduce by the result of comparative example 1 and comparative example 2 and react temperature
After degree, be advantageous to the separation of n-alkane, n-alkane mass fraction substantially reduces in oil phase product 111, octane number RON results
Also significantly improve.
Claims (8)
1. a kind of method for improving octane number, comprises the following steps：
(1) gasoline is through the isolated light component oil of weight component and heavy constituent oil；
(2) the heavy constituent oil mixes with enveloping agent solution, carries out complex reaction, filtered to obtain liquid-phase product and solid phase production
Product；
(3) liquid-phase product obtains oil phase product through washing；
(4) light component is oily obtains product oil with the oil phase product mix, that is, improves octane number.
2. according to the method for claim 1, it is characterised in that：In step (1), the gasoline is catalytically cracked gasoline, is evaporated
Journey is 30~220 DEG C；
The temperature of the weight component separation is 70~120 DEG C.
3. method according to claim 1 or 2, it is characterised in that：In step (2), the network of the enveloping agent solution use
Mixture for it is following 1) or 2)：
1) thiocarbamide, biuret or biruea；
2) urea and mixture any in thiocarbamide, biuret and biruea；
The mass ratio of the urea and the thiocarbamide, the biuret or the biruea is 1：1~5；
Solvent in the enveloping agent solution is ethanol, mass fraction is 95% ethanol water, methanol, propyl alcohol, butanol, third
Ketone or butanone.
4. according to the method any one of claim 1-3, it is characterised in that：In step (2), in the enveloping agent solution
The mass ratio of complexing agent and the heavy constituent oil be 1~5：1~5；
The temperature of the complex reaction is -30~15 DEG C.
5. according to the method any one of claim 1-4, it is characterised in that：In step (3), the washing adds water
Quality is 1~3 times of the liquid-phase product quality.
6. according to the method any one of claim 1-5, it is characterised in that：Methods described also includes producing the solid phase
The step of product are handled as follows：
Be dissolved in water the solids product, is isolated to aqueous phase and oil phase product A；
The oil phase product A obtains oil phase product B and rinse water through washing.
7. according to the method for claim 6, it is characterised in that：The aqueous phase is isolated to the complexing agent.
8. the method according to claim 6 or 7, it is characterised in that：The quality for dissolving the solids product addition water is institute
State solids product quality 1~3 times；
The temperature of the dissolving is 20~80 DEG C；
The quality that the washing adds water is 1~3 times of the oil phase product A mass.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711047651.6A CN107779221B (en) | 2017-10-31 | 2017-10-31 | Method for separating normal paraffin from gasoline and improving gasoline octane number |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711047651.6A CN107779221B (en) | 2017-10-31 | 2017-10-31 | Method for separating normal paraffin from gasoline and improving gasoline octane number |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107779221A true CN107779221A (en) | 2018-03-09 |
| CN107779221B CN107779221B (en) | 2020-04-17 |
Family
ID=61431752
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711047651.6A Active CN107779221B (en) | 2017-10-31 | 2017-10-31 | Method for separating normal paraffin from gasoline and improving gasoline octane number |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107779221B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096034A (en) * | 2018-07-17 | 2018-12-28 | 天津大学 | The new process and device of coupling reaction and separation separation normal hydrocarbon and isohydrocarbon |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1058954A (en) * | 1990-08-16 | 1992-02-26 | 岳阳石油化工总厂研究院 | The novel method of normal fatty acid and positive structure hydrocarbon in the Separation by Complexation crude naphthenic acid |
| CN104312619A (en) * | 2014-11-03 | 2015-01-28 | 黑龙江科技大学 | Method for separating n-alkane from shale oil |
| CN105567320A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | High-octane number low-sulfur gasoline production method |
-
2017
- 2017-10-31 CN CN201711047651.6A patent/CN107779221B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1058954A (en) * | 1990-08-16 | 1992-02-26 | 岳阳石油化工总厂研究院 | The novel method of normal fatty acid and positive structure hydrocarbon in the Separation by Complexation crude naphthenic acid |
| CN105567320A (en) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | High-octane number low-sulfur gasoline production method |
| CN104312619A (en) * | 2014-11-03 | 2015-01-28 | 黑龙江科技大学 | Method for separating n-alkane from shale oil |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096034A (en) * | 2018-07-17 | 2018-12-28 | 天津大学 | The new process and device of coupling reaction and separation separation normal hydrocarbon and isohydrocarbon |
| CN109096034B (en) * | 2018-07-17 | 2021-09-03 | 天津大学 | Process and device for separating normal hydrocarbon and isomeric hydrocarbon by reaction separation coupling |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107779221B (en) | 2020-04-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP3459651B2 (en) | Synthetic diesel fuel and method for producing the same | |
| CN103214332B (en) | Method for producing light aromatic hydrocarbons and high-quality oil products from catalytically cracked diesel | |
| US20180298294A1 (en) | Systems and methods for producing fuel intermediates | |
| CN109705915A (en) | A kind of catalyst cracking method of fecund iso-butane and light aromatics | |
| CN102676212A (en) | Raw oil optimization method for improving environment-friendly rubber filling oil aromatic hydrocarbon content and equipment | |
| Xu et al. | Participation of methane in an economically and environmentally favorable catalytic asphaltene upgrading process | |
| CN110229692B (en) | Compound solvent for separating cycloparaffin and arene from naphtha and preparation method and application thereof | |
| CN102863988B (en) | Coal tar combined machining method | |
| CN107779221A (en) | A kind of method that n-alkane improves octane number in separation gasoline | |
| CN102676214B (en) | Solvent refining method and equipment for producing environmental-protection rubber filling oil | |
| CN106467760B (en) | A kind of processing of heavy oil method | |
| CN108822885B (en) | Composite extracting agent for Fischer-Tropsch oil deoxidizer and preparation method thereof | |
| RU2153523C1 (en) | High-octane gasoline production process | |
| CN108779399B (en) | Process and catalyst for producing high octane components | |
| CN103059999A (en) | Paraffin production method | |
| CN108504382B (en) | Compound solvent for separating cyclane and arene from naphtha, preparation method and application thereof | |
| Махмудов et al. | COLLOIDAL-CHEMICAL FEATURES OF SURFACTANTS AND ADDITIVES INTO LOW OCTANE GASOLINES TO IMPROVE THEIR QUALITY | |
| CN105567320B (en) | A kind of production method of high-octane rating low-sulphur oil | |
| RU2441055C2 (en) | Method of pollution-free fuel | |
| CN105712848B (en) | A kind of methyl tertiary butyl ether(MTBE) desulfurizing agent and its application method | |
| CN105567317B (en) | A kind of production method of high-octane rating low-sulphur oil | |
| CN105567313B (en) | A kind of production method of high-octane rating low-sulphur oil | |
| CN113122326B (en) | Deep desulfurization method for full-fraction catalytic cracking gasoline | |
| RU2108367C1 (en) | Gasoline production process | |
| RU2133260C1 (en) | Method of preparing plasticizer, plasticizer |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 101407 No.1, south 2nd Yueyuan street, C District, Yanqi Economic Development Zone, Huairou District, Beijing Patentee after: Zhongke synthetic oil Technology Co.,Ltd. Address before: 101407 No.1, south 2nd Yueyuan street, C District, Yanqi Economic Development Zone, Huairou District, Beijing Patentee before: SYNFUELS CHINA TECHNOLOGY Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder |