CN101774882A - Method for catalytic hydrodechlorination of CFC125 into HFC-125 - Google Patents
Method for catalytic hydrodechlorination of CFC125 into HFC-125 Download PDFInfo
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- CN101774882A CN101774882A CN201010004079A CN201010004079A CN101774882A CN 101774882 A CN101774882 A CN 101774882A CN 201010004079 A CN201010004079 A CN 201010004079A CN 201010004079 A CN201010004079 A CN 201010004079A CN 101774882 A CN101774882 A CN 101774882A
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- hfc
- cfc
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- catalytic hydrogenation
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- GTLACDSXYULKMZ-UHFFFAOYSA-N pentafluoroethane Chemical compound FC(F)C(F)(F)F GTLACDSXYULKMZ-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000003197 catalytic effect Effects 0.000 title abstract 3
- RFCAUADVODFSLZ-UHFFFAOYSA-N 1-Chloro-1,1,2,2,2-pentafluoroethane Chemical compound FC(F)(F)C(F)(F)Cl RFCAUADVODFSLZ-UHFFFAOYSA-N 0.000 claims abstract description 54
- 235000019406 chloropentafluoroethane Nutrition 0.000 claims abstract description 54
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 40
- 239000003054 catalyst Substances 0.000 claims description 36
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims description 15
- 238000006298 dechlorination reaction Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 14
- 230000008569 process Effects 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims description 2
- 239000000377 silicon dioxide Substances 0.000 claims description 2
- 239000004480 active ingredient Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 description 35
- 230000009466 transformation Effects 0.000 description 13
- 239000006227 byproduct Substances 0.000 description 12
- 239000012495 reaction gas Substances 0.000 description 11
- UJPMYEOUBPIPHQ-UHFFFAOYSA-N 1,1,1-trifluoroethane Chemical group CC(F)(F)F UJPMYEOUBPIPHQ-UHFFFAOYSA-N 0.000 description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 8
- 238000002360 preparation method Methods 0.000 description 5
- 101150003085 Pdcl gene Proteins 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000005303 weighing Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- BOSAWIQFTJIYIS-UHFFFAOYSA-N 1,1,1-trichloro-2,2,2-trifluoroethane Chemical compound FC(F)(F)C(Cl)(Cl)Cl BOSAWIQFTJIYIS-UHFFFAOYSA-N 0.000 description 1
- BAMUEXIPKSRTBS-UHFFFAOYSA-N 1,1-dichloro-1,2,2,2-tetrafluoroethane Chemical compound FC(F)(F)C(F)(Cl)Cl BAMUEXIPKSRTBS-UHFFFAOYSA-N 0.000 description 1
- BOUGCJDAQLKBQH-UHFFFAOYSA-N 1-chloro-1,2,2,2-tetrafluoroethane Chemical compound FC(Cl)C(F)(F)F BOUGCJDAQLKBQH-UHFFFAOYSA-N 0.000 description 1
- VEZJSKSPVQQGIS-UHFFFAOYSA-N 1-chloro-2-fluoroethane Chemical class FCCCl VEZJSKSPVQQGIS-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000000779 depleting effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for the catalytic hydrodechlorination of CFC125 into HFC-125. Under optimized reaction conditions, the method can lead the conversion rate of the CFC-115 to over 90% and simultaneously maintain the selectivity of the HFC-125 over 95%. The method for the catalytic hydrodechlorination of CFC125 into OFD-substitutes HFC-125 has great industrial application prospect.
Description
Technical field
The present invention relates to a kind of CFC-115 (1,1,1,2,2-five fluoro-2-monochlorethanes) catalytic hydrogenation and dechlorination continuous production HFC-125 (1,1,1,2,2-pentafluoride ethane) method is the method for catalyst CFC-115 hydrodechlorination continuous production HFC-125 with Pd/C on fixed-bed reactor specifically.
Background technology
Depletion of the ozone layer is one of key subjects of world today's environment protection.At present, the ozone hole in the South Pole has expanded to more than 2,700 ten thousand square kilometres, and the ultraviolet radiation increase that brings thus causes great harm for the living environment of human society.Chlorofluorocarbons (CFCs) (CFCs) is the main ozone-depleting material (ODS) of a class, and CFC-115 is as a kind of important CFCs species, and its ODP (ODP) is 0.6.Must before 2010, stop the consumption and the discharging of CFCs class ozone-depleting material according to Montreal protocol China.China is in the consumption of ozonosphere depleting substances such as regulation complete prohibition on July 1st, 2007 freonll-11.The ideal substitute of CFC-115 is HFC-125, and its ODP (ODP) is 0.0.A kind of ideal method is by catalytic hydrogenation and dechlorination CFC-115 to be converted into HFC-125.Set up the successful conversion that process that a step hydrodechlorination prepares HFC-125 can realize CFC-115 by this method in the CFC-115 technical process existing production, to satisfy the research and development demand that continues with permanent production technology, greatly reduce the investment of producing ODS substitute HFC-125, thereby realize the green smooth transition of domestic existing CFC-115 technological process.In addition, produce in the HFC-125 process existing, CFC-115 is still as main by product, the purity that improves the HFC-125 product needs by the rectification under vacuum mode CFC-115 to be separated, this process is accompanied by very high energy consumption, and isolated CFC-115 still need handle, and is less economical, and the CFC-115 of by-product is converted into HFC-125 by the hydrodechlorination reaction, then have high economic benefit.
People such as Moon (Applied Catalysis A:General, 1998,168,159-170) reported Pd has been loaded on the different carriers preparation loading type Pd catalyzer, and investigate the hydrodechlorination activity of its CFC-115, but the Pd/C catalyzer is not specialized in the document, and the hydrodechlorination activity of the Pd/C catalyzer of report is lower.Subsequently people such as Thompson (Journal of Physical Chemistry B, 2000,104,3067-3077) reported the hydrodechlorination reaction mechanism of CFC-115, HCFC-124, CFC-114a and CFC-113a on the Pd/C catalyzer.The document does not propose the Pd/C catalyzer is applied to CFC-115 hydrodechlorination system HFC-125, is not optimized at this reaction pair catalyzer yet.
The invention provides a kind of CFC-115 catalytic hydrogenation and dechlorination and produce the method for HFC-125, overcome the lower defective of hydrodechlorination activity of Pd/C catalyzer, CFC-115 transformation efficiency and HFC-125 selectivity all can be reached more than 90%.
Summary of the invention
The object of the present invention is to provide a kind of CFC-115 catalytic hydrogenation and dechlorination to produce the method for HFC-125, especially be applied to the conversion of CFC-115 in the HFC-125 gas mixture of suitability for industrialized production.
Realize that the object of the invention technical scheme is: in fixed-bed reactor, adopt the Pd/C catalyzer, carry out the CFC-115 catalytic hydrogenation and dechlorination through following steps and produce HFC-125:
1) catalyst pretreatment: catalyzer is packed in the reactor, feeds a certain proportion of H under certain air speed
2And N
2Gas mixture reduces for some time at a certain temperature.
2) catalyzed reaction: behind the catalyst pretreatment, feed reactor feed gas and H in the reactor
2Gas mixture carry out hydrodechlorination reaction at a certain temperature.
3) aftertreatment: reacted gas obtains product through alkali lye absorption, silica dehydrator pipe after dewatering.
The H that feeds in the catalyst pretreatment in the step 1 wherein
2With N
2H in the gas mixture
2Volumn concentration be 1-10%.The catalyst pretreatment temperature is 300-400 ℃.The catalyst pretreatment time is 2-4h.The total air speed of catalyst pretreatment gas mixture is 1200-3600ml g
-1(catal.) h
-1
Reaction pressure is a normal pressure in the step 2, and temperature of reaction is 280-350 ℃, and reaction velocity is 600-4000ml g
-1(catal.) h
-1, reactor feed gas and H
2The ratio of volume is: 1: 2-1: 8.Under optimized reaction conditions, the CFC-115 transformation efficiency and the HFC-125 selectivity of this reaction all can reach more than 90%.
Embodiment
Further describe feature of the present invention below by example, but the present invention is not limited to following example.
[embodiment 1]
Preparation of Catalyst: take by weighing 0.0417g PdCl
2, add a small amount of concentrated hydrochloric acid dissolving back adding secondary water and be configured to H
2PdCl
4The aqueous solution joins the 5g gac, and obtaining the Pd charge capacity after the drying is the Pd/C catalyzer of 0.5wt.%.
Catalyzed reaction is carried out on fixed-bed reactor, and Pd/C catalyzer loading capacity is 0.5g, and catalyzer and thinner quartz sand (40-60 order) weight ratio is 1: 4, is loaded in the crystal reaction tube behind the mixing.Before reaction, logical in advance H
2: N
2Gas mixture (H
2Volume content 1%), online reduction 3h under 350 ℃, the total air speed of gas mixture is 3600ml g
-1(catal.) h
-1
After pre-treatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is 320 ℃.The CFC-115 transformation efficiency is 7.2% after the stable reaction, and the HFC-125 selectivity is 100%.
[embodiment 2]
Preparation of Catalyst: take by weighing 0.1667g PdCl
2, add a small amount of concentrated hydrochloric acid dissolving back adding secondary water and be configured to H
2PdCl
4The aqueous solution joins the 5g gac, and obtaining the Pd charge capacity after the drying is the Pd/C catalyzer of 2wt.%.
Loaded catalyst and pretreatment mode are with embodiment 1, and difference is H
2: N
2H in the gas mixture
2Volume content is 10%, and temperature is 300 ℃, and the time is 2h, and air speed is 1200mlg
-1(catal.) h
-1
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is 320 ℃.The CFC-115 transformation efficiency is 68.9% after the stable reaction, and the HFC-125 selectivity is 96.6%, and main by product is HFC-143a.
[embodiment 3]
Preparation of Catalyst: take by weighing 0.2334g PdCl
2, add a small amount of concentrated hydrochloric acid dissolving back adding secondary water and be configured to H
2PdCl
4The aqueous solution joins the 5g gac, and obtaining the Pd charge capacity after the drying is the Pd/C catalyzer of 2.8wt.%.
Loaded catalyst and pretreatment mode are with embodiment 1.Difference is at H
2: N
2H in the gas mixture
2Volume content is 5%, and air speed is 2400ml g
-1(catal.) h
-1
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 97.5% after the stable reaction, and the HFC-125 selectivity is 96.7%, and main by product is HFC-143a.
[embodiment 4]
Preparation of Catalyst: take by weighing 0.4168g PdCl
2, add a small amount of concentrated hydrochloric acid dissolving back adding secondary water and be configured to H
2PdCl
4The aqueous solution joins the 5g gac, and obtaining the Pd charge capacity after the drying is the Pd/C catalyzer of 5wt.%.
Loaded catalyst and pretreatment mode are with embodiment 1, and difference is H
2: N
2H in the gas mixture
2Volume content 5%, temperature are 400 ℃, and the time is 4h, and air speed is 2400mlg
-1(catal.) h
-1
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 95.6% after the stable reaction, and the HFC-125 selectivity is 92.6%, and main by product is HFC-143a.
[embodiment 5]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is: 350 ℃.The CFC-115 transformation efficiency is 98.2% after the stable reaction, and the HFC-125 selectivity is 90.5%, and main by product is HFC-143a.
[embodiment 6]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is: 280 ℃.The CFC-115 transformation efficiency is 60.3% after the stable reaction, and the HFC-125 selectivity is 98.1%, and main by product is HFC-143a.
[embodiment 7]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 1200ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 80.5% after the stable reaction, and the HFC-125 selectivity is 97.4%, and main by product is HFC-143a.
[embodiment 8]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 2400ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 68.4% after the stable reaction, and the HFC-125 selectivity is 97.8%, and main by product is HFC-143a.
[embodiment 9]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 2, total air speed is 3600ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 59.2% after the stable reaction, and the HFC-125 selectivity is 98.5%, and main by product is HFC-143a.
[embodiment 10]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 4, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 98.2% after the stable reaction, and the HFC-125 selectivity is 97.1%, and main by product is HFC-143a.
[embodiment 11]
It is the Pd/C of 2.8wt.% that catalyzer is selected the Pd charge capacity for use, and loaded catalyst and pretreatment mode are with embodiment 1.
After catalyst pretreatment finished, switching gas was reactor feed gas, and the reaction gas proportioning is CFC-115 and H
2Volume ratio be 1: 6, total air speed is 600ml g
-1(catal.) h
-1, temperature of reaction is: 320 ℃.The CFC-115 transformation efficiency is 98.4% after the stable reaction, and the HFC-125 selectivity is 97.9%, and main by product is HFC-143a.
。
Claims (9)
1. a CFC-115 catalytic hydrogenation and dechlorination is produced the method for HFC-125.It is characterized in that this catalyzed reaction process following steps:
1) catalyst pretreatment: catalyzer is packed in the reactor, feeds a certain proportion of H under certain air speed
2And N
2Gas mixture reduces for some time at a certain temperature.
2) catalyzed reaction: behind the catalyst pretreatment, feed reactor feed gas and H in the reactor
2Gas mixture carry out hydrodechlorination reaction at a certain temperature.
3) aftertreatment: reacted gas obtains product through alkali lye absorption, silica dehydrator pipe after dewatering.
2. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, it is characterized in that the H that feeds in the step 1
2With N
2H in the gas mixture
2Volumn concentration be 1-10%.
3. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, it is characterized in that the catalyst pretreatment temperature is 300-400 ℃ in the step 1.
4. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, it is characterized in that the catalyst pretreatment time is 2-6h in the step 1.
5. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, it is characterized in that catalyst pretreatment gas mixture air speed is 1200-3600mlg in the step 1
-1(catal.) h
-1
6. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, it is characterized in that temperature of reaction is 280-350 ℃ in the step 2.
7. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, it is characterized in that reaction velocity is 600-4000ml g in the step 2
-1(catal.) h
-1
8. CFC-115 catalytic hydrogenation and dechlorination according to claim 1 is produced the method for HFC-125, reactor feed gas and H in it is characterized in that reacting in the step 2
2The ratio of volume is: 1: 2-1: 8.
9. a kind of method that the CFC-115 catalytic hydrogenation and dechlorination is produced HFC-125 that is used for according to claim 1 is characterized in that described catalyzer is the Pd/C catalyzer, and wherein the charge capacity of active ingredient Pd is 0.05-5wt.%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010004079A CN101774882A (en) | 2010-01-21 | 2010-01-21 | Method for catalytic hydrodechlorination of CFC125 into HFC-125 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010004079A CN101774882A (en) | 2010-01-21 | 2010-01-21 | Method for catalytic hydrodechlorination of CFC125 into HFC-125 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101774882A true CN101774882A (en) | 2010-07-14 |
Family
ID=42511500
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010004079A Pending CN101774882A (en) | 2010-01-21 | 2010-01-21 | Method for catalytic hydrodechlorination of CFC125 into HFC-125 |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101774882A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977744A (en) * | 2014-06-05 | 2014-08-13 | 西安凯立化工有限公司 | Method for catalytic degradation of hexachlorobenzene |
| CN106336343A (en) * | 2016-08-19 | 2017-01-18 | 山东东岳化工有限公司 | Method for reducing R115 in R125 |
| CN110092703A (en) * | 2018-01-31 | 2019-08-06 | 上海汇友精密化学品有限公司 | A kind of preparation method of pentafluoroethane |
-
2010
- 2010-01-21 CN CN201010004079A patent/CN101774882A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977744A (en) * | 2014-06-05 | 2014-08-13 | 西安凯立化工有限公司 | Method for catalytic degradation of hexachlorobenzene |
| CN103977744B (en) * | 2014-06-05 | 2016-02-03 | 西安凯立新材料股份有限公司 | A kind of method of catalytic degradation hexachloro-benzene |
| CN106336343A (en) * | 2016-08-19 | 2017-01-18 | 山东东岳化工有限公司 | Method for reducing R115 in R125 |
| CN110092703A (en) * | 2018-01-31 | 2019-08-06 | 上海汇友精密化学品有限公司 | A kind of preparation method of pentafluoroethane |
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Correction item: Applicant Correct: Fluoro-Chemial Co., Ltd., Quzhou, Zhejiang Prov False: Zhejiang Normal University Number: 28 Volume: 26 |
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Correction item: Applicant Correct: Fluoro-Chemial Co., Ltd., Quzhou, Zhejiang Prov False: Zhejiang Normal University Number: 28 Page: The title page Volume: 26 |
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Free format text: CORRECT: APPLICANT; FROM: ZHEJIANG QUHUA FLUORINE CHEMICAL CO., LTD. TO: FLUORO-CHEMIAL CO LTD, QUZHOU, ZHEJIANG PROV |
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Application publication date: 20100714 |